CN103121908A - Method for separating mesitylene via extractive distillation - Google Patents
Method for separating mesitylene via extractive distillation Download PDFInfo
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- CN103121908A CN103121908A CN2011103723140A CN201110372314A CN103121908A CN 103121908 A CN103121908 A CN 103121908A CN 2011103723140 A CN2011103723140 A CN 2011103723140A CN 201110372314 A CN201110372314 A CN 201110372314A CN 103121908 A CN103121908 A CN 103121908A
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- extractive distillation
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- AUHZEENZYGFFBQ-UHFFFAOYSA-N mesitylene Substances CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000000895 extractive distillation Methods 0.000 title claims abstract description 37
- 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 abstract description 4
- 239000002904 solvent Substances 0.000 claims abstract description 67
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000000926 separation method Methods 0.000 claims abstract description 29
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims abstract description 10
- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 claims abstract description 4
- 238000000605 extraction Methods 0.000 claims description 28
- 238000004821 distillation Methods 0.000 claims description 24
- 125000003118 aryl group Chemical group 0.000 claims description 19
- 239000000203 mixture Substances 0.000 claims description 15
- 239000000470 constituent Substances 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 9
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000006317 isomerization reaction Methods 0.000 claims description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 2
- 239000006227 byproduct Substances 0.000 claims description 2
- 238000005336 cracking Methods 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 238000002407 reforming Methods 0.000 claims description 2
- 239000008096 xylene Substances 0.000 claims description 2
- 230000008901 benefit Effects 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000000126 substance Substances 0.000 abstract description 6
- 239000000047 product Substances 0.000 description 12
- 238000009835 boiling Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 7
- 239000002994 raw material Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- NIQCNGHVCWTJSM-UHFFFAOYSA-N Dimethyl phthalate Chemical compound COC(=O)C1=CC=CC=C1C(=O)OC NIQCNGHVCWTJSM-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000000638 solvent extraction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004508 fractional distillation Methods 0.000 description 3
- KWVPRPSXBZNOHS-UHFFFAOYSA-N 2,4,6-Trimethylaniline Chemical compound CC1=CC(C)=C(N)C(C)=C1 KWVPRPSXBZNOHS-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- QMKYBPDZANOJGF-UHFFFAOYSA-N benzene-1,3,5-tricarboxylic acid Chemical compound OC(=O)C1=CC(C(O)=O)=CC(C(O)=O)=C1 QMKYBPDZANOJGF-UHFFFAOYSA-N 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- FBSAITBEAPNWJG-UHFFFAOYSA-N dimethyl phthalate Natural products CC(=O)OC1=CC=CC=C1OC(C)=O FBSAITBEAPNWJG-UHFFFAOYSA-N 0.000 description 2
- 229960001826 dimethylphthalate Drugs 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000006277 sulfonation reaction Methods 0.000 description 2
- QZZSAWGVHXXMID-UHFFFAOYSA-N 1-amino-4-bromo-9,10-dioxoanthracene-2-sulfonic acid Chemical compound C1=CC=C2C(=O)C3=C(Br)C=C(S(O)(=O)=O)C(N)=C3C(=O)C2=C1 QZZSAWGVHXXMID-UHFFFAOYSA-N 0.000 description 1
- OMRXVBREYFZQHU-UHFFFAOYSA-N 2,4-dichloro-1,3,5-triazine Chemical compound ClC1=NC=NC(Cl)=N1 OMRXVBREYFZQHU-UHFFFAOYSA-N 0.000 description 1
- VSAWBBYYMBQKIK-UHFFFAOYSA-N 4-[[3,5-bis[(3,5-ditert-butyl-4-hydroxyphenyl)methyl]-2,4,6-trimethylphenyl]methyl]-2,6-ditert-butylphenol Chemical compound CC1=C(CC=2C=C(C(O)=C(C=2)C(C)(C)C)C(C)(C)C)C(C)=C(CC=2C=C(C(O)=C(C=2)C(C)(C)C)C(C)(C)C)C(C)=C1CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 VSAWBBYYMBQKIK-UHFFFAOYSA-N 0.000 description 1
- RGCKGOZRHPZPFP-UHFFFAOYSA-N Alizarin Natural products C1=CC=C2C(=O)C3=C(O)C(O)=CC=C3C(=O)C2=C1 RGCKGOZRHPZPFP-UHFFFAOYSA-N 0.000 description 1
- SGHZXLIDFTYFHQ-UHFFFAOYSA-L Brilliant Blue Chemical compound [Na+].[Na+].C=1C=C(C(=C2C=CC(C=C2)=[N+](CC)CC=2C=C(C=CC=2)S([O-])(=O)=O)C=2C(=CC=CC=2)S([O-])(=O)=O)C=CC=1N(CC)CC1=CC=CC(S([O-])(=O)=O)=C1 SGHZXLIDFTYFHQ-UHFFFAOYSA-L 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
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- 239000012847 fine chemical Substances 0.000 description 1
- PAGLBVQGOBETSU-UHFFFAOYSA-N formaldehyde 1,2,3-trimethylbenzene Chemical compound O=C.CC1=CC=CC(C)=C1C PAGLBVQGOBETSU-UHFFFAOYSA-N 0.000 description 1
- 230000002363 herbicidal effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
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- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
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- KKZJGLLVHKMTCM-UHFFFAOYSA-N mitoxantrone Chemical compound O=C1C2=C(O)C=CC(O)=C2C(=O)C2=C1C(NCCNCCO)=CC=C2NCCNCCO KKZJGLLVHKMTCM-UHFFFAOYSA-N 0.000 description 1
- 229960001156 mitoxantrone Drugs 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
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- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
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- 230000002195 synergetic effect Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for separating mesitylene via extractive distillation, wherein an extractive distillation solvent adopted in the method is one of N-methyl-2-pyrrolidone and 2-pyrrolidone, and preferably is N-methyl-2-pyrrolidone. The method disclosed by the invention has the advantages of being relatively simple in separation process, low in operating energy consumption, and high in product yield. The extractive distillation solvent adopted in the method is high in separation efficiency for mesitylene and o-methyl-ethylbenzene, so that the separation process can be realized on an extractive distillation tower with few tower plates; and moreover, the solvent is easy to recover and good in chemical thermostability.
Description
Technical field
The present invention relates to chemical field, say further, relate to a kind of method of separation of extractive distillation sym-trimethylbenzene.
Background technology
Sym-trimethylbenzene is a kind of fine chemical material of preciousness, through nitrated, hydrogenating reduction, produces 2,4,6-trimethylaniline, then with the condensation of Isosorbide-5-Nitrae dihydroxyanthraquinone, sulfonation, generate the slightly acidic gorgeous blue RAW in pula; Another kind of dyestuff be sym-trimethylbenzene through sulfonation, nitrated, reduction, make 2,4-diamino-sym-trimethylbenzene-6-sulfonic acid, be condensed into blue color base with bromamine acid again, then with the reaction of oxyethyl group dichloro s-triazine, generate at last reactive brilliant blue K-3R and RAN, be used for stamp and pad dyeing; 2,4,6-trimethylaniline and the condensation of alpha-chloro methyl propionate, can be made into cornfield herbicidal in addition, is made into 20% solution and uses.In addition, can be made into antioxidant 330 take sym-trimethylbenzene as raw material, trimesic acid, multiple Chemicals and the chemical intermediates such as 2,4,6-, three cresols also can be for the synthesis of the trimethylbenzene formaldehyde resins, and its purposes is wide, and added value is very high.Sym-trimethylbenzene 10% left and right in oil at the bottom of refinery reformer benzenol hydrorefining.This part reformation carbon nine resource of China further do not develop always at present, take the Chang Ling refinery as example, this factory produces approximately 0.7 ten thousand tons of sym-trimethylbenzene per year at present, if be isolated purification, petroleum resources are rationally utilized, also can increase the economic benefit of enterprise.
Because the boiling point of each component in the C9 aromatic mixture is very approaching, particularly sym-trimethylbenzene and adjacent methyl-ethyl benzene boiling point are only poor approximately 0.5 ℃, relative volatility is 1.009, larger with the conventional distillation separating difficulty, if with the conventional distillation method, it is separated, need thousands of theoretical stages, therefore be actually and realize.
Up to now, people have developed many methods that prepare sym-trimethylbenzene, mainly contain the kinds of processes such as unsym-trimethyl benzene isomerization method, extraction fractional distillation, molecular sieve absorption process, complexing/partition method, alkylation-partition method, the raw material that above technique adopts all derives from the C9 aromatic cut.It is reported, in above-mentioned method, the extraction fractional distillation product yield is higher, and solvent is reused, and does not produce refuse, can comprehensive utilization of C
9Aromatic hydrocarbon resource, and there is no environmental issue is compared with other method and is had many-sided advantage, has very high commercial value.The extraction fractional distillation ultimate principle is the effect by selective solvent, changes the relative volatility between sym-trimethylbenzene and o-methylethylbenzene, thereby reaches the purpose of purification sym-trimethylbenzene.Therefore, extraction distillation solvent plays a part crux to sym-trimethylbenzene and adjacent methyl-ethyl benzene separation efficiency in the technico-economical comparison of sepn process.
US Patent No. 3220933 has disclosed with dimethyl phthalate as extraction solvent, to C
9Aromatic hydrocarbons carries out extractive distillation, because this solvent is not good to the separating effect of sym-trimethylbenzene and o-methylethylbenzene, only can obtain 87% sym-trimethylbenzene, well below 98% (purity of sym-trimethylbenzene first grade).domestic Nanjing Normal University to the method carried out further research (extracting rectifying is produced the experimental study of sym-trimethylbenzene. during chemical industry the periodical .2000, 5:18～20.), by experimental result as can be known, when reflux ratio is 4, the mass ratio of solvent and raw material feed material is 10 o'clock, extractive distillation column number of theoretical plate N is under the condition of 102, the massfraction of the sym-trimethylbenzene material in overhead distillate can reach more than 0.92, and this process has been carried out analog calculation, analog calculation shows, when with N=170, the massfraction of the sym-trimethylbenzene material under equal conditions in overhead distillate just can reach more than 98%, adopt dimethyl phthalate to prepare the required extracting rectifying column plate of highly purified sym-trimethylbenzene number requirement too high (N=170) as extraction solvent, solvent/material rate is excessive.
Chinese patent CN1958538A discloses a kind of method that double solvent extraction separates C9 aromatic, comprises the C9 aromatic mixture is carried out prefractionation, and intercepting contains the enriched fraction of sym-trimethylbenzene and o-methylethylbenzene; The middle part that will contain the enriched fraction introducing double solvent extraction rectifying tower of sym-trimethylbenzene and o-methylethylbenzene, high boiling solvent injects from described double solvent extraction rectifier, low boiling point solvent is from the bottom injection of described double solvent extraction rectifying tower, under two kinds of solvent synergistic extraction effects, tower top obtains containing the mixed fraction of sym-trimethylbenzene and low boiling point solvent, obtains containing the mixed fraction of section's o-methylethylbenzene and high boiling solvent at the bottom of tower; Two bursts of mixed fraction of tower top and tower reactor gained are separated in solvent recovery tower respectively, sym-trimethylbenzene and adjacent methyl-ethyl benzene product that separation obtains are discharged system, reuse after two kinds of solvent recuperation.Owing to having introduced again a kind of solvent, must separate and recycle this solvent, thereby need to increase a low boiling point solvent knockout tower.The shortcoming that equipment one-time investment and flow process relative complex are arranged.In addition, discharge due to low boiling point solvent and sym-trimethylbenzene with from tower top, cause the sepn process energy consumption to increase.
Chinese patent CN1513818A reported a kind of rectifying in extraction crossing in conjunction with separation of C
9Technique, adopt the N-N-formyl morpholine N-as extraction distillation solvent, in overhead distillate, the content of sym-trimethylbenzene can reach more than 98.5%, because this solvent is lower to the separation efficiency of sym-trimethylbenzene and adjacent methyl-ethyl benzene, nearly 123 of extractive distillation column number of theoretical plate N, the sym-trimethylbenzene yield is only 84%.Therefore, for solving the problems of the prior art, a kind of method of separation of extractive distillation sym-trimethylbenzene is provided, and it is very necessary having the method that lock out operation is relatively simple, operation energy consumption is low, product yield is high and invest lower separation of extractive distillation sym-trimethylbenzene.
Summary of the invention
For solving the problems of the prior art, the invention provides a kind of method of separation of extractive distillation sym-trimethylbenzene, have advantages of that separating technology is relatively simple, operation energy consumption is low, product yield is high, the extraction distillation solvent that the method is utilized is high to the separation efficiency between sym-trimethylbenzene and adjacent methyl-ethyl benzene, its sepn process is easily realized on the less extractive distillation column of stage number, and this solvent is easy to reclaim, chemical heat is stablized.
A kind of method that the purpose of this invention is to provide separation of extractive distillation sym-trimethylbenzene.
The extraction distillation solvent that described method adopts is a kind of in METHYLPYRROLIDONE, 2-Pyrrolidone, is preferably METHYLPYRROLIDONE.
The inventor is through deep research, a large amount of extraction distillation solvents that are used for the separation of extractive distillation sym-trimethylbenzene have been screened, surprised discovery, contain the nitrogen compound METHYLPYRROLIDONE, 2-Pyrrolidone can change the relative volatility between sym-trimethylbenzene and o-methylethylbenzene significantly, and compare with the solvent compositions that contains inorganic salt, has not blocking pipe, advantage simple to operate.
Described method comprises:
(1) the C9 aromatic mixture through removing light constituent is introduced the unsym-trimethyl benzene tower, tower top is discharged the enriched fraction that contains sym-trimethylbenzene and methyl-ethyl benzene, and tower reactor is drawn the logistics that contains sym-trimethylbenzene;
(2) the unsym-trimethyl benzene column overhead being discharged the enriched fraction that contains sym-trimethylbenzene and methyl-ethyl benzene introduces from the middle part of extractive distillation column, described extraction distillation solvent is introduced from tower top, through after extracting rectifying, sym-trimethylbenzene is discharged from the top of extractive distillation column, discharges the logistics that contains o-methylethylbenzene and solvent at the bottom of tower;
(3) with discharging the logistics that contains o-methylethylbenzene and solvent at the bottom of the extractive distillation column tower, introduce solvent recovery tower, contain o-methylethylbenzene and get logistics from the discharge of solvent recuperation tower top, extraction distillation solvent is discharged rear recycle at the bottom of solvent recovery tower.
Wherein, by weight, the 0.5-12 of the enriched fraction inlet amount that described extraction distillation solvent consumption is described sym-trimethylbenzene and methyl-ethyl benzene times, preferred 3-8 doubly;
(1) light constituent of the C9 aromatic mixture that removes light constituent in the step refers to boiling point less than the component of sym-trimethylbenzene, is mainly isopropyl benzene, n-proplbenzene,, to methyl-ethyl benzene.(1) method that removes light constituent in the C9 aromatic mixture in the step can adopt precise distillation of the prior art or extraction and distillation technology.
Operational condition can adopt common operational condition in this area, can be preferred in the present invention:
The theoretical plate number of described unsym-trimethyl benzene tower is 60-100, and trim the top of column is than being 10-20, and tower top temperature is 150-170 ℃, and column bottom temperature is 170-200 ℃, and tower top pressure is 0.08-0.12MPa, and tower bottom pressure is 0.09-0.14MPa.
The theoretical plate number of described extractive distillation column is 70-120, and trim the top of column is than being 2-5, and tower top temperature is 150-170 ℃, and column bottom temperature is 190-220 ℃, and tower top pressure is 0.08-0.12MPa, and tower bottom pressure is 0.09-0.14MPa.
The theoretical plate number of described recovery tower is 10-20, and the reflux ratio of tower top is 1-3, and tower top temperature is 155-170 ℃, and column bottom temperature is 190-230 ℃, and tower top pressure is 0.08-0.12MPa, and tower bottom pressure is 0.09-0.14MPa.
Described C9 aromatic mixture can be preferably from oil, xylene isomerization by-product, cycle oil or cracking naphtha at the bottom of the platinum reforming tower, wherein the content of sym-trimethylbenzene is 8 % by weight-50 % by weight, the content of adjacent methyl-ethyl benzene is 5 % by weight-50 % by weight, and the content of unsym-trimethyl benzene is 8 % by weight-60 % by weight.The C9 aromatic of different sources forms slightly different, can regulate flow process and operational means according to practical situation.
Method of the present invention has the following advantages: solvent is high to the separation efficiency between sym-trimethylbenzene and adjacent methyl-ethyl benzene,
1, the solvent that adopts due to the method is high to the separation efficiency of sym-trimethylbenzene and adjacent methyl-ethyl benzene, the separation of sym-trimethylbenzene can be realized on the less extractive distillation column of stage number, but also reduced extraction distillation solvent consumption (having reduced the mass ratio of the enriched fraction of solvent/sym-trimethylbenzene and methyl-ethyl benzene), can reach investment less, the purpose that the production process energy consumption is lower.
2, adopt method of the present invention, the sym-trimethylbenzene yield that obtains is significantly improved, and has therefore improved the economic benefit of obtaining the sym-trimethylbenzene product from C9 aromatic.
Description of drawings
Fig. 1: separation of extractive distillation sym-trimethylbenzene schematic flow sheet of the present invention
Description of reference numerals
Equipment class: T1 unsym-trimethyl benzene tower, T2 extractive distillation column, T3 solvent recovery tower
The logistics class: 1 removes the C9 aromatic mixture of light constituent, the enriched fraction of 2 sym-trimethylbenzene and methyl-ethyl benzene, and 3 unsym-trimethyl benzenes, 4 sym-trimethylbenzene, 5 o-methylethylbenzenes and solvent, 6 mainly contain the logistics of o-methylethylbenzene, 7 circulating solvents
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As shown in Figure 1, the C9 aromatic mixture 1 through removing light constituent enters the middle and lower part of unsym-trimethyl benzene tower T1, and tower top is discharged the enriched fraction 2 that contains sym-trimethylbenzene and section's methyl-ethyl benzene, and tower reactor is drawn the logistics 3 that mainly contains sym-trimethylbenzene; Enter the middle and lower part of extractive distillation column T2 from the enriched fraction 2 that contains sym-trimethylbenzene and section's methyl-ethyl benzene of T1 tower top outflow, circulating solvent 7 enters extractive distillation column T2 by top, through separation of extractive distillation, tower top distillates sym-trimethylbenzene 4, discharges the logistics 5 that mainly contains o-methylethylbenzene and solvent at the bottom of tower; The logistics that mainly contains o-methylethylbenzene and solvent 5 of discharging from the T2 tower reactor is introduced into solvent recovery tower, and the logistics 6 that mainly contains o-methylethylbenzene is discharged from the solvent recuperation tower top, and extraction distillation solvent 7 is discharged rear recycle at the bottom of solvent recovery tower.
Extraction distillation solvent used is METHYLPYRROLIDONE;
In embodiment, raw material used is the C9 aromatic mixture that removes light constituent, wherein contains the sym-trimethylbenzene of 35.10 % by weight, and its concrete component and content see Table 1.
Table 1 removes C9 aromatic compositions of mixtures and the boiling point of light constituent
| The component title | Content (% by weight) | Boiling point (℃) |
| Light constituent | 0.40 | - |
| Sym-trimethylbenzene | 35.10 | 164.74 |
| O-methylethylbenzene | 38.10 | 165.18 |
| Unsym-trimethyl benzene | 26.40 | 169.38 |
The yield of product calculates by following formula:
Yield and the purity of concrete separating technology condition, each logistics explanation, product are seen table 2, table 3, table 4.
The separating technology condition of table 2 embodiment
Each logistics explanation of table 3 embodiment
Each product yield and the purity of table 4 embodiment
| Unsym-trimethyl benzene yield (% by weight) | O-methylethylbenzene yield (% by weight) | Sym-trimethylbenzene yield (% by weight) |
| 98.50 | 99.51 | 93.20 |
| Unsym-trimethyl benzene purity (% by weight) | O-methylethylbenzene purity (% by weight) | Sym-trimethylbenzene purity (% by weight) |
| 99.3 | 93.38 | 98.5 |
Comparative Examples:
Raw material used is the C9 aromatic mixture that removes light constituent, wherein contains the sym-trimethylbenzene of 35.10 % by weight, and its concrete component and content see Table 1.
Extraction distillation solvent adopts the specially N-N-formyl morpholine N-of CN1513818A profit disclosure of China.By Fig. 1 described from C9 aromatic the method for enriched mesitylene implement, the yield of concrete separating technology condition, each logistics explanation, product and purity see Table 5, table 6, table 7.
The separating technology condition of table 5 Comparative Examples
Each logistics explanation of table 6 Comparative Examples
Each product yield and the purity of table 7 Comparative Examples
| Unsym-trimethyl benzene yield (% by weight) | O-methylethylbenzene yield (% by weight) | Sym-trimethylbenzene yield (% by weight) |
| 98.50 | 99.8 | 82.8 |
| Unsym-trimethyl benzene is received purity (% by weight) | O-methylethylbenzene purity (% by weight) | Sym-trimethylbenzene purity (% by weight) |
| 99.3 | 85.90 | 98.50 |
From table 2,5 as can be known, owing to adopting the higher extraction distillation solvent of separation efficiency, solvent/raw material (weight rate ratio) is reduced to 7 from 10, thereby has reduced energy consumption; In addition, from table 4,7 as can be known, owing to adopting the higher extraction distillation solvent of separation efficiency, product sym-trimethylbenzene yield brings up to 93.2% from 82.3%, has therefore improved the economic benefit of obtaining the sym-trimethylbenzene product from C9 aromatic.
Claims (7)
1. the method for a separation of extractive distillation sym-trimethylbenzene is characterized in that:
The extraction distillation solvent that described method adopts is a kind of in METHYLPYRROLIDONE, 2-Pyrrolidone.
2. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 1 is characterized in that:
Described extraction distillation solvent is METHYLPYRROLIDONE.
3. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 1 or 2 is characterized in that: said method comprising the steps of:
(1) the C9 aromatic mixture through removing light constituent is introduced the unsym-trimethyl benzene tower, tower top is discharged the enriched fraction that contains sym-trimethylbenzene and methyl-ethyl benzene, and tower reactor is drawn the logistics that contains sym-trimethylbenzene;
(2) the unsym-trimethyl benzene column overhead being discharged the enriched fraction that contains sym-trimethylbenzene and methyl-ethyl benzene introduces from the middle part of extractive distillation column, described extraction distillation solvent is introduced from tower top, through after extracting rectifying, sym-trimethylbenzene is discharged from the top of extractive distillation column, discharges the logistics that contains o-methylethylbenzene and solvent at the bottom of tower;
(3) with discharging the logistics that contains o-methylethylbenzene and solvent at the bottom of the extractive distillation column tower, introduce solvent recovery tower, contain o-methylethylbenzene and get logistics from the discharge of solvent recuperation tower top, extraction distillation solvent is discharged rear recycle at the bottom of solvent recovery tower.
4. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 3 is characterized in that:
The 0.5-12 of the enriched fraction inlet amount that described extraction distillation solvent consumption is described sym-trimethylbenzene and methyl-ethyl benzene doubly.
5. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 4 is characterized in that:
The 3-8 of the enriched fraction inlet amount that described extraction distillation solvent consumption is described sym-trimethylbenzene and methyl-ethyl benzene doubly.
6. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 3 is characterized in that:
The theoretical plate number of described extractive distillation column is 70-120, and trim the top of column is than being 2-5, and tower top temperature is 150-170 ℃, and column bottom temperature is 190-220 ℃, and tower top pressure is 0.08-0.12MPa, and tower bottom pressure is 0.09-0.14MPa.
7. the method for separation of extractive distillation sym-trimethylbenzene as claimed in claim 3 is characterized in that:
Described C9 aromatic mixture from the platinum reforming tower at the bottom of oil, xylene isomerization by-product, cycle oil or cracking naphtha, wherein the content of sym-trimethylbenzene is 8 % by weight-50 % by weight, the content of adjacent methyl-ethyl benzene is 5 % by weight-50 % by weight, and the content of unsym-trimethyl benzene is 8 % by weight-60 % by weight.
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| CN104591952A (en) * | 2014-12-25 | 2015-05-06 | 天津大学 | Method for refining mesitylene by virtue of differential pressure thermal coupling rectification |
| CN105542834A (en) * | 2014-10-30 | 2016-05-04 | 中国石化扬子石油化工有限公司 | Composite solvent for extraction distillation separation of aromatic hydrocarbons, and applications thereof |
| CN105837394A (en) * | 2016-04-05 | 2016-08-10 | 天津大学 | Purifying method of highly-pure 1,2,3-trimethylbenzene |
| CN109627140A (en) * | 2017-10-09 | 2019-04-16 | 中国石化扬子石油化工有限公司 | A kind of mesitylene extraction and rectification separation method |
| CN111886062A (en) * | 2018-11-01 | 2020-11-03 | 株式会社Lg化学 | Method for separating organic solvent from mixed solution containing organic solvent |
| 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 |
| CN114213208A (en) * | 2021-12-31 | 2022-03-22 | 黄河三角洲京博化工研究院有限公司 | Method for extracting, rectifying and purifying mesitylene by using efficient composite solvent |
| CN114292155A (en) * | 2021-12-31 | 2022-04-08 | 黄河三角洲京博化工研究院有限公司 | Method for thermally coupling and purifying mesitylene |
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| CN105542834A (en) * | 2014-10-30 | 2016-05-04 | 中国石化扬子石油化工有限公司 | Composite solvent for extraction distillation separation of aromatic hydrocarbons, and applications thereof |
| CN104591952A (en) * | 2014-12-25 | 2015-05-06 | 天津大学 | Method for refining mesitylene by virtue of differential pressure thermal coupling rectification |
| CN105837394A (en) * | 2016-04-05 | 2016-08-10 | 天津大学 | Purifying method of highly-pure 1,2,3-trimethylbenzene |
| CN105837394B (en) * | 2016-04-05 | 2018-12-21 | 天津大学 | A kind of method of purification of high-purity 1,2,3-trimethylbenzene |
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| CN114213208A (en) * | 2021-12-31 | 2022-03-22 | 黄河三角洲京博化工研究院有限公司 | Method for extracting, rectifying and purifying mesitylene by using efficient composite solvent |
| CN114292155A (en) * | 2021-12-31 | 2022-04-08 | 黄河三角洲京博化工研究院有限公司 | Method for thermally coupling and purifying mesitylene |
| CN114213208B (en) * | 2021-12-31 | 2024-01-30 | 黄河三角洲京博化工研究院有限公司 | Method for extracting, rectifying and purifying mesitylene by high-efficiency composite solvent |
| CN114292155B (en) * | 2021-12-31 | 2024-05-03 | 黄河三角洲京博化工研究院有限公司 | Method for purifying mesitylene through thermal coupling |
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