CN100494132C - Method for preparing mixed methylnaphthalene by using C+10 heavy aromatic hydrocarbon as raw material - Google Patents
Method for preparing mixed methylnaphthalene by using C+10 heavy aromatic hydrocarbon as raw material Download PDFInfo
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- CN100494132C CN100494132C CNB2008100246881A CN200810024688A CN100494132C CN 100494132 C CN100494132 C CN 100494132C CN B2008100246881 A CNB2008100246881 A CN B2008100246881A CN 200810024688 A CN200810024688 A CN 200810024688A CN 100494132 C CN100494132 C CN 100494132C
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- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000002994 raw material Substances 0.000 title claims description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 26
- 238000010992 reflux Methods 0.000 claims abstract description 26
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000002904 solvent Substances 0.000 claims abstract description 8
- 241000282326 Felis catus Species 0.000 claims description 18
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 2
- 210000001190 lateral line system Anatomy 0.000 claims description 2
- QIMMUPPBPVKWKM-UHFFFAOYSA-N 2-methylnaphthalene Chemical compound C1=CC=CC2=CC(C)=CC=C21 QIMMUPPBPVKWKM-UHFFFAOYSA-N 0.000 abstract description 28
- 239000007788 liquid Substances 0.000 abstract description 5
- 238000002360 preparation method Methods 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 2
- 238000004821 distillation Methods 0.000 abstract 12
- 239000000463 material Substances 0.000 abstract 2
- 239000012467 final product Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 9
- 239000011280 coal tar Substances 0.000 description 7
- 125000001424 substituent group Chemical group 0.000 description 7
- 238000009835 boiling Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 3
- BFIMMTCNYPIMRN-UHFFFAOYSA-N 1,2,3,5-tetramethylbenzene Chemical compound CC1=CC(C)=C(C)C(C)=C1 BFIMMTCNYPIMRN-UHFFFAOYSA-N 0.000 description 2
- FYGHSUNMUKGBRK-UHFFFAOYSA-N 1,2,3-trimethylbenzene Chemical compound CC1=CC=CC(C)=C1C FYGHSUNMUKGBRK-UHFFFAOYSA-N 0.000 description 2
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 2
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 239000000975 dye Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- UOHMMEJUHBCKEE-UHFFFAOYSA-N prehnitene Chemical compound CC1=CC=C(C)C(C)=C1C UOHMMEJUHBCKEE-UHFFFAOYSA-N 0.000 description 2
- 238000007639 printing Methods 0.000 description 2
- 238000009941 weaving Methods 0.000 description 2
- AUHZEENZYGFFBQ-UHFFFAOYSA-N 1,3,5-trimethylbenzene Chemical compound CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 description 1
- FZTYGIKSBFTSNW-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound CC1=CC=CC2=CC=CC=C12.CC1=CC=CC2=CC=CC=C12 FZTYGIKSBFTSNW-UHFFFAOYSA-N 0.000 description 1
- QWDFCPOBZPRCDC-UHFFFAOYSA-N 1-methylnaphthalene;2-methylnaphthalene Chemical compound C1=CC=CC2=CC(C)=CC=C21.C1=CC=C2C(C)=CC=CC2=C1 QWDFCPOBZPRCDC-UHFFFAOYSA-N 0.000 description 1
- HLMGIACBRPHDBD-UHFFFAOYSA-N CC1=CC2=CC=CC=C2C=C1.CC1=CC2=CC=CC=C2C=C1 Chemical compound CC1=CC2=CC=CC=C2C=C1.CC1=CC2=CC=CC=C2C=C1 HLMGIACBRPHDBD-UHFFFAOYSA-N 0.000 description 1
- 229930003448 Vitamin K Natural products 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 235000019219 chocolate Nutrition 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- SHUZOJHMOBOZST-UHFFFAOYSA-N phylloquinone Natural products CC(C)CCCCC(C)CCC(C)CCCC(=CCC1=C(C)C(=O)c2ccccc2C1=O)C SHUZOJHMOBOZST-UHFFFAOYSA-N 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000000984 vat dye Substances 0.000 description 1
- 235000019168 vitamin K Nutrition 0.000 description 1
- 239000011712 vitamin K Substances 0.000 description 1
- 150000003721 vitamin K derivatives Chemical class 0.000 description 1
- 229940046010 vitamin k Drugs 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A method for preparing mixed methylnaphthalene from C10 heavy Aromatic Hydrocarbon material belongs to the preparation technical field of alpha and beta-methylnaphthalene, which comprises leading C10 heavy Aromatic Hydrocarbon material from the inlet of a first distillation column into the first distillation column at normal temperature to be distilled, controlling the top temperature, pressure, reflux ratio and bottom heating temperature of the first distillation column, exchanging the heat and condensing the light fraction at the top of the first distillation column, feeding the condensate into a first column top reflux tank, leading out the top distillate of the first distillation column as solvent, leading out liquid naphthalene at the side pipeline of the first distillation column, leading the heavy fraction at the bottom of the first distillation column into a second distillation column to be distilled further, controlling the top temperature, pressure and reflux ratio and bottom heating temperature of the second distillation column, exchanging the heat and condensing the light fraction of the second distillation column, feeding the condensate into a seond column top reflux tank to obtain the final product of mixed methylnaphthalene, and leading out the heavy fraction at the bottom of the second distillation column from the bottom of the second distillation column. The invention has simple process, simple operation, low cost and non generation of three wastes in whole preparation.
Description
Technical field
The invention belongs to the preparing technical field of α, beta-methylnaphthalene, be specifically related to a kind of method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene.
Background technology
Mixed methylnaphthalene mainly is the mixture of alpha-methyl-naphthalene and beta-methylnaphthalene, i.e. the mixture of 1-methylnaphthalene and 2-methylnaphthalene.The 1-methylnaphthalene claims alpha-methyl-naphthalene again, and the 2-methylnaphthalene claims beta-methylnaphthalene, because methylnaphthalene is the monobasic substituent of naphthalene, and the name of the monobasic substituent of naphthalene is again to name for the basis according to the parent nucleus of naphthalene, and is specific as follows:
The molecular structural formula of naphthalene is:
Generally write the structural formula of naphthalene the form of as (1).Wherein 1,4,5,8 four carbon atoms all are adjacent with the public carbon atom of two phenyl ring, are referred to as the α position usually, and any one hydrogen atom is substituted and all obtains identical monobasic substituent on these four positions, is referred to as the α substituent.2,3,6,7 four positions also equate, are referred to as β-position, and the hydrogen atom on β-position is substituted and then obtains the beta substitution thing.Therefore the monobasic substituent of naphthalene has α-and β-two kind of isomer.Methylnaphthalene is exactly the monobasic substituent of menaphthyl reaction, and two kinds of isomer of alpha-methyl-naphthalene and beta-methylnaphthalene are just arranged in the substituent, and both structural formulas are as follows:
Alpha-methyl-naphthalene (1-methylnaphthalene) beta-methylnaphthalene (2-methylnaphthalene)
Although both molecular formula are identical, all be C
11H
10, molecular weight is all 142.20, but both physical and chemical performances are absolutely different:
Alpha-methyl-naphthalene: boiling point ℃ 241-243; Fusing point ℃-22; Proportion 1.001; Flash-point ℃ 82.
Beta-methylnaphthalene: boiling point ℃ 241-242; Fusing point ℃ 34-36; Proportion 1.000; Flash-point ℃ 97.
Mixed methylnaphthalene mainly is the mixture of alpha-methyl-naphthalene and beta-methylnaphthalene, and the raw material as proposing beta-methylnaphthalene also can be used as high-grade baking vanish, printing ink etc.Methylnaphthalene is a kind of broad-spectrum fine chemical product, for industries such as weaving, printing and dyeing, papermaking crucial meaning is arranged.Wherein alpha-methyl-naphthalene is mainly used in and produces dispersed dye, reactive dyestuffs, the dispersion agent of vat dyes, levelling agent, the dispersion agent of aviation spraying agricultural chemicals, and the water reducer of cement concrete, for example:
And beta-methylnaphthalene is mainly used in the making vitamin K, medicine, dyestuff, weaving etc.
Mixed methylnaphthalene is mainly derived from coal tar and Petroleum Aromatics.Coal tar claims coal cream again, is that obtain in the dry distillation of coal process a kind of has special odor, flammable and mordant black or chocolate viscous liquid.Coal tar contains up to ten thousand kinds of compositions, form very complicated, naphthalene from the isopropyl benzene of 152.4 ℃ of boiling points to 217.96 ℃ of boiling points, in 65.56 ℃ boiling spread, just there are 37 kinds of compounds, moreover with a kind of compound a plurality of isomer are arranged again exactly, for example Three methyl Benzene just has sym-trimethylbenzene, unsym-trimethyl benzene and hemimellitene; Tetramethyl-benzene just has durol for another example, isodurene and prenitol, and so on, so it is very difficult therefrom to isolate monomer.The methylnaphthalene component that comes from coal tar usually needs through overpickling, take off quinoline obtains thick methylnaphthalene pregnant solution, and then deep processing prepares methylnaphthalene (referring to the process patent 96117039 from coal tar crude refining beta-methyl naphthalene-methylnaphthalene).Although contain α, beta-methylnaphthalene in the coal tar distillate of complicated composition, normally used method all exists problems such as complex process, energy consumption are big, equipment corrosion, environmental pollution, so α, beta-methylnaphthalene are that mixed methylnaphthalene is basically from external import.Along with the comprehensive development and utilization of carrying out in a deep going way of coal tar comprehensive process, particularly C+10 heavy aromatic hydrocarbon, thereby the mixed methylnaphthalene that belongs to the high-end product category of high added value is had a good application prospect.The technical scheme that the present invention will introduce below is based on producing under this background.
Summary of the invention
Task of the present invention is will provide that a kind of not only technology is simple, energy consumption is low, realize easily but also to the environment method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene of influence not.
Task of the present invention is finished like this, a kind of method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene, it is that the C+10 heavy aromatic hydrocarbon raw material is incorporated into rectifying first rectifying tower from the opening for feed of first rectifying tower at normal temperatures, control the first rectifying tower tower top temperature respectively, tower top pressure, Heating temperature at the bottom of reflux ratio and the tower, the first rectifying tower cat head light fraction is after heat exchange and condensation, phlegma enters first return tank of top of the tower, the first rectifying tower overhead product leads to solvent through pipeline, the lateral line canal pass fluid naphthalene of first rectifying tower, and heavy fraction is introduced further rectifying in second rectifying tower at the bottom of the first rectifying Tata, control the second rectifying tower tower top temperature, tower top pressure, Heating temperature at the bottom of reflux ratio and the tower, the second rectifying tower cat head light fraction is after heat exchange and condensation, phlegma enters second return tank of top of the tower, obtain the mixed methylnaphthalene finished product, heavy fraction is drawn at the bottom of the second rectifying Tata at the bottom of the second rectifying Tata, wherein: the described control first rectifying tower tower top temperature is that temperature is controlled to be 110～120 ℃, the described control first rectifying tower tower top pressure is meant that the control absolute pressure is 10～15KPa, the described control first rectifying tower reflux ratio is to be 1: 6～1:12 with control of reflux ratio, and Heating temperature is meant the Heating temperature of well heater at the bottom of the control first rectifying Tata at the bottom of the described control first rectifying Tata; The described control second rectifying tower tower top temperature is that temperature is controlled to be 155～165 ℃, the described control second rectifying tower tower top pressure is meant that the control absolute pressure is 20～25KPa, the described control second rectifying tower reflux ratio is to be 1: 6～1: 12 with control of reflux ratio, and Heating temperature is meant the Heating temperature of well heater at the bottom of the control second rectifying Tata at the bottom of the described control second rectifying Tata.
In a specific embodiment of the present invention, the content of methylnaphthalene is 35～40% in the described C+10 heavy aromatic hydrocarbon raw material.
Go back in the specific embodiment of the present invention, well heater is for adopting hydronic first reboiler of thermal oil at the bottom of the described first rectifying Tata, and the temperature of thermal oil is 270～295 ℃.
In another specific embodiment of the present invention, described solvent is 1500
#Solvent.
In another specific embodiment of the present invention, well heater is for adopting hydronic second reboiler of thermal oil at the bottom of the described second rectifying Tata, and the temperature of thermal oil is 270～295 ℃.
Method processing step disclosed by the invention is few, easy and simple to handle; Owing to utilized the C+10 heavy aromatic hydrocarbon that is often used as fuel, therefore not only raw material sources easily and belong to the comprehensive utilization of C+10 heavy aromatic hydrocarbon, so cost is low; There is not the three wastes factor that undermines environment in whole process of preparation.
Description of drawings
Accompanying drawing is the synoptic diagram of the present invention by the method equipment therefor of C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene.
Embodiment
Embodiment 1:
Ask for an interview accompanying drawing, the methylnaphthalene content that to discuss square 26A5 of luxuriant century Nanjing source of a specified duration petrochemical industry company limited for No. 49 available from south of the mountains road in the NanJing City, Jiangsu Province,China is 35.3% C+10 heavy aromatic hydrocarbon raw material, and be 1.2m by pipeline 1 from diameter at normal temperatures with this raw material, tower height is 35m, stage number is that the middle and lower part opening for feed of 112 first rectifying tower 2 is introduced first rectifying tower 2 and carried out rectifying, control of reflux ratio is 1:10, the cat head absolute pressure is controlled to be 10KPa, tower top temperature is controlled to be 112 ℃, first rectifying tower, 2 cat head light fractions liquid after 3 coolings of the first cat head interchanger enters in first return tank of top of the tower 4 of first rectifying tower 2, uncooled part enters further condensation in first overhead condenser 5 of first rectifying tower 2, phlegma enters in first return tank of top of the tower 4 of first rectifying tower 2, and the overhead product of first rectifying tower 2 is 1500
#Solvent is also drawn through first pipeline 6, the overhead product that the side line pipeline 7 of the middle and lower part of first rectifying tower 2 is drawn is the liquid naphthalene, the heavy fraction of first rectifying tower 2 enters at the bottom of the tower and by the heat-conducting oil heating of first reboiler 8 through 272 ℃, forming the circulation heating evaporation returns at the bottom of the tower light constituent that wherein contains, to be incorporated into diameter by the tower bottom tube road 9 of first rectifying tower 2 be 1.0m to heavy fraction at the bottom of the first rectifying Tata, tower height is 28m, stage number is 90 second rectifying tower, 10 further rectifying, the reflux ratio of controlling second rectifying tower 10 is 1:12, the cat head absolute pressure is 23KPa, tower top temperature is 165 ℃, the heavy fraction of second rectifying tower 10 enters at the bottom of the tower and by the heat-conducting oil heating of second reboiler 11 through 274 ℃, form the circulation heating evaporation, the light constituent that wherein contains is returned at the bottom of the tower, heavy fraction is drawn subsequent processing by the second tower bottom tube road 12 of second rectifying tower 10 and is further processed, the cat head light fraction of second rectifying tower 10 liquid after the second cat head interchanger, 13 heat exchange cooling enters in second return tank of top of the tower 14 of second rectifying tower 10, and uncooled partially liq enters condensation in second overhead condenser 15 of second rectifying tower 10, enter after the condensation in second return tank of top of the tower 14 of second rectifying tower 10, draw the finished product mixed methylnaphthalene through second pipeline 16.
Embodiment 2:
Only the content of methylnaphthalene in the C+10 heavy aromatic hydrocarbon raw material is changed into 2 controls of 36.1%, the first rectifying tower: reflux ratio changes 1:8, cat head absolute pressure into and changes 15Kpa, tower top temperature into and change that the heat-conducting oil heating temperature is 295 ℃ at the bottom of 120 ℃, tower into; The control of second rectifying tower 10: the heat-conducting oil heating temperature changed 292 ℃ at the bottom of reflux ratio changed 1:6, cat head absolute pressure into and changes 20Kpa, tower top temperature into and change 156 ℃, tower into.All the other are with embodiment 1.
Embodiment 3:
Only the content of methylnaphthalene in the C+10 heavy aromatic hydrocarbon raw material is changed into 2 controls of 37.5%, the first rectifying tower: reflux ratio changes 1: 10 into, the cat head absolute pressure changes 13Kpa into, tower top temperature changes that the heat-conducting oil heating temperature is 280 ℃ at the bottom of 119 ℃, tower into; The control of second rectifying tower 10: the heat-conducting oil heating temperature changed 281 ℃ at the bottom of reflux ratio changed 1:9, cat head absolute pressure into and changes 22Kpa, tower top temperature into and change 160 ℃, tower into.All the other are with embodiment 1.
Embodiment 4:
Only the content of methylnaphthalene in the C+10 heavy aromatic hydrocarbon raw material is changed into 2 controls of 38.8%, the first rectifying tower: reflux ratio changes 1:7, cat head absolute pressure into and changes 12Kpa, tower top temperature into and change that the heat-conducting oil heating temperature is 285 ℃ at the bottom of 115 ℃, tower into; The control of second rectifying tower 10: the heat-conducting oil heating temperature was for changing 280 ℃ at the bottom of reflux ratio changed 1:8, cat head absolute pressure into and changes 25Kpa, tower top temperature into and change 165 ℃, tower into.All the other are with embodiment 1.
Embodiment 5:
Only the content of methylnaphthalene in the C+10 heavy aromatic hydrocarbon raw material is changed into 2 controls of 40.0%, the first rectifying tower: reflux ratio changes 1:12, cat head absolute pressure into and changes 13Kpa, tower top temperature into and change that the heat-conducting oil heating temperature is 294 ℃ at the bottom of 120 ℃, tower into; The control of second rectifying tower 10: the heat-conducting oil heating temperature changed 290 ℃ at the bottom of reflux ratio changed 1:10, cat head absolute pressure into and changes 20Kpa, tower top temperature into and change 158 ℃, tower into.All the other are with embodiment 1.
The finished product mixed methylnaphthalene content analysis that above-mentioned all embodiment make is reflected by following table.
The finished product mixed methylnaphthalene of each embodiment is analyzed
| The embodiment sequence number | Alpha-methyl-naphthalene content % | Beta-methylnaphthalene content % | Mixed methylnaphthalene total content % |
| 1 | 10.0 | 50.8 | 60.8 |
| 2 | 13.5 | 51.5 | 65.0 |
| 3 | 18.6 | 54.6 | 73.2 |
| 4 | 19.8 | 58.5 | 78.3 |
| 5 | 16.4 | 63.9 | 80.3 |
By the foregoing description as seen, in the process by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene, except that the entrucking of finished product mixed methylnaphthalene, other processes all are under the air tight condition carries out, and this has not only improved utilization ratio of raw materials greatly simultaneously also will drop to bottom line to environment and operator's influence.
Claims (5)
1, a kind of method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene, it is characterized in that it is that the C+10 heavy aromatic hydrocarbon raw material is incorporated into rectifying first rectifying tower from the opening for feed of first rectifying tower at normal temperatures, control the first rectifying tower tower top temperature respectively, tower top pressure, Heating temperature at the bottom of reflux ratio and the tower, the first rectifying tower cat head light fraction is after heat exchange and condensation, phlegma enters first return tank of top of the tower, the first rectifying tower overhead product leads to solvent through pipeline, the lateral line canal pass fluid naphthalene of first rectifying tower, and heavy fraction is introduced further rectifying in second rectifying tower at the bottom of the first rectifying Tata, control the second rectifying tower tower top temperature, tower top pressure, Heating temperature at the bottom of reflux ratio and the tower, the second rectifying tower cat head light fraction is after heat exchange and condensation, phlegma enters second return tank of top of the tower, obtain the mixed methylnaphthalene finished product, heavy fraction is drawn at the bottom of the second rectifying Tata at the bottom of the second rectifying Tata, wherein: the described control first rectifying tower tower top temperature is that temperature is controlled to be 110～120 ℃, the described control first rectifying tower tower top pressure is meant that the control absolute pressure is 10～15KPa, the described control first rectifying tower reflux ratio is to be 1: 6～1: 12 with control of reflux ratio, and Heating temperature is meant the Heating temperature of well heater at the bottom of the control first rectifying Tata at the bottom of the described control first rectifying Tata; The described control second rectifying tower tower top temperature is that temperature is controlled to be 155～165 ℃, the described control second rectifying tower tower top pressure is meant that the control absolute pressure is 20～25KPa, the described control second rectifying tower reflux ratio is to be 1: 6～1: 12 with control of reflux ratio, and Heating temperature is meant the Heating temperature of well heater at the bottom of the control second rectifying Tata at the bottom of the described control second rectifying Tata.
2, the method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene according to claim 1, the content that it is characterized in that methylnaphthalene in the described C+10 heavy aromatic hydrocarbon raw material is 35～40%.
3, the method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene according to claim 1 is characterized in that well heater is for adopting hydronic first reboiler of thermal oil at the bottom of the described first rectifying Tata, and the temperature of thermal oil is 270～295 ℃.
4, the method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene according to claim 1 is characterized in that described solvent is 1500
#Solvent.
5, the method by C+10 heavy aromatic hydrocarbon feedstock production mixed methylnaphthalene according to claim 1 is characterized in that well heater is for adopting hydronic second reboiler of thermal oil at the bottom of the described second rectifying Tata, and the temperature of thermal oil is 270～295 ℃.
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| CN108531210A (en) * | 2018-03-05 | 2018-09-14 | 常熟联邦化工股份有限公司 | A kind of preparation method of high methyl naphthalene aromatic solvent naphtha |
| CN109293464B (en) * | 2018-11-19 | 2021-07-09 | 鹏辰新材料科技股份有限公司 | Method for effectively separating and purifying 2-methylnaphthalene from wash oil |
| CN114832416B (en) * | 2022-04-01 | 2023-07-14 | 中国成达工程有限公司 | Mixed aromatic hydrocarbon vacuum rectification system and method for producing durene |
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Non-Patent Citations (2)
| Title |
|---|
| 重整C10重芳烃的综合利用. 张洪涛等.当代化工，第30卷第3期. 2001 |
| 重整C10重芳烃的综合利用. 张洪涛等.当代化工，第30卷第3期. 2001 * |
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