CN102078699A - Direct distillation technology for 2-methylnaphthalene - Google Patents
Direct distillation technology for 2-methylnaphthalene Download PDFInfo
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- CN102078699A CN102078699A CN2009102272264A CN200910227226A CN102078699A CN 102078699 A CN102078699 A CN 102078699A CN 2009102272264 A CN2009102272264 A CN 2009102272264A CN 200910227226 A CN200910227226 A CN 200910227226A CN 102078699 A CN102078699 A CN 102078699A
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- negative pressure
- methylnaphthalene
- tower
- methyl naphthalene
- extraction
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- QIMMUPPBPVKWKM-UHFFFAOYSA-N 2-methylnaphthalene Chemical compound C1=CC=CC2=CC(C)=CC=C21 QIMMUPPBPVKWKM-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 238000004821 distillation Methods 0.000 title claims abstract description 17
- 238000005516 engineering process Methods 0.000 title abstract description 6
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 claims abstract description 36
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 9
- 238000000605 extraction Methods 0.000 claims description 32
- 241000282326 Felis catus Species 0.000 claims description 21
- 238000000034 method Methods 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 238000006116 polymerization reaction Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract 1
- 239000002904 solvent Substances 0.000 description 3
- 239000000284 extract Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Abstract
The invention discloses a direct distillation technology for 2-methylnaphthalene, which comprises the following steps: A. removing naphthalene fractions from the mixed methylnaphthalene at the top of the primary distillation tower (1) and then directly introducing a tower bottom liquid into a negative pressure flash evaporator (2) for separation; B. extracting the mixed methylnaphthalene from the bottom of the negative pressure flash evaporator (2) and 2-methylnaphthalene fractions from the tower top of the negative pressure flash evaporator (2); and C. extracting the 2- methylnaphthalene fractions from the tower top of the negative pressure flash evaporator (2) to enter into a negative pressure rectifying tower (3) for carrying out the negative pressure rectification, and finally extracting the mixed methylnaphthalene from the tower bottom of the negative pressure rectifying tower (3) and the 2-methylnaphthalene from the tower top of the negative pressure rectifying tower (3). The amount of the extracted 2-methylnaphthalene in the invention reaches 97%, and the annual output of a single device reaches 2400 tons. What is more, the emission amount of the three wastes is less and can be eliminated automatically, thus being a clean and zero release production technology.
Description
Technical field
The present invention relates to a kind of distil process, be specifically related to a kind of direct distil process of 2-methyl naphthalene.
Background technology
At present, extracting the common method that adopts of 2-methyl naphthalene from washing oil is the distillations of six stoves, six tower normal pressure continous ways.But this kind technological process is long, is unfavorable for production control, and energy consumption is big, and recovery rate is low, and output is little, can only extract 95% 2-methyl naphthalene.The another kind of method that adopts usually is: the solvent way of distillation.This kind technology has increased the consumption of solvent, has increased cost, has increased the solvent recovery process, and has produced waste liquid, causes the environmental protection difficulty.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of simplification and the extraction process of 2-methyl naphthalene efficiently.
Technical scheme of the present invention is: a kind of direct distil process of 2-methyl naphthalene comprises following processing step:
After A, mixed methylnaphthalene cut the naphthalene cut from normal pressure primary distillation tower cat head, liquid directly entered the vacuum flash device and separates under keeping warm mode at the bottom of the tower;
B, from vacuum flash device bottom extraction mixed methylnaphthalene, from vacuum flash device cat head extraction 2-methylnaphthalene;
C, enter the negative pressure rectifying column from vacuum flash device cat head extraction 2-methylnaphthalene, carry out negative pressure rectifying, extraction mixed methylnaphthalene at the bottom of the negative pressure rectifying Tata is from negative pressure rectifying column cat head extraction 2-methyl naphthalene.
Among the described step C at the bottom of the negative pressure rectifying Tata extraction mixed methylnaphthalene enter the raw material tank reuse.
The tower top pressure of described normal pressure primary distillation tower is a normal pressure, and tower top temperature is 215 ℃～225 ℃, and reflux ratio is 10～15.
The vacuum of described negative pressure rectifying column tower top pressure is 80～90%, and tower top temperature is 150 ℃～170 ℃, and reflux ratio is 10～15.
Enter catalyst converter from negative pressure rectifying column cat head extraction 2-methyl naphthalene among the described step C, allow the micro constitutent catalytic polymerization, and discharge, enter separator (5), isolate the 2-methyl naphthalene from the 2-methyl naphthalene of catalyst converter top extraction by the catalyst converter bottom.
Described discharge liquid of discharging from the catalyst converter bottom enters factory's incinerator or heat-conducting oil furnace burns.
The invention has the beneficial effects as follows: the 2-methyl naphthalene content that the present invention extracts reaches 97%, and single covering device output is for producing 2400 tons per year.Can be used as commodity selling from the mixed methylnaphthalene of vacuum flash device bottom extraction, from vacuum flash device cat head can extraction 90% the 2-methylnaphthalene, from the cat head of negative pressure rectifying column can extraction 96% the 2-methyl naphthalene, can isolate 97% 2-methyl naphthalene from separator.Technology of the present invention is simple, the product yield height, technological process is short, be convenient to strict middle index control, make product quality secure, and improved the thermal efficiency and energy utilization rate, and this technological process three waste discharge is few, only discharging also can digest voluntarily, has accomplished the process for cleanly preparing of zero-emission substantially.
Description of drawings
Fig. 1 is a process chart of the present invention;
Fig. 2 is the A partial enlarged drawing of Fig. 1;
Fig. 3 is the B partial enlarged drawing of Fig. 1;
Fig. 4 is the C partial enlarged drawing of Fig. 1;
Fig. 5 is the D partial enlarged drawing of Fig. 1;
Fig. 6 is the E partial enlarged drawing of Fig. 1.
The specific embodiment
A kind of direct distil process of 2-methyl naphthalene, processing step is as follows:
After A, mixed methylnaphthalene cut the naphthalene cut from normal pressure primary distillation tower (1) cat head, liquid directly entered vacuum flash device (2) and separates under keeping warm mode at the bottom of the tower;
B, from vacuum flash device (2) bottom extraction mixed methylnaphthalene, from vacuum flash device (2) cat head extraction 2-methylnaphthalene;
C, enter negative pressure rectifying column (3) from vacuum flash device (2) cat head extraction 2-methylnaphthalene, carry out negative pressure rectifying, the extraction mixed methylnaphthalene enters the raw material tank reuse at the bottom of negative pressure rectifying column (3) tower, from negative pressure rectifying column (3) cat head extraction 2-methyl naphthalene.
D, enter catalyst converter (4) from negative pressure rectifying column (3) cat head extraction 2-methyl naphthalene, allow the micro constitutent catalytic polymerization, and by the discharge of catalyst converter (4) bottom, the discharge liquid of discharging enters factory's incinerator or heat-conducting oil furnace burns, enter separator (5) from the 2-methyl naphthalene of catalyst converter (4) top extraction, isolate the 2-methyl naphthalene.
In the present embodiment, the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 215 ℃, and reflux ratio is 10.The vacuum of negative pressure rectifying column (3) tower top pressure is 85%, and tower top temperature is 150 ℃, and reflux ratio is 10.
A kind of direct distil process of 2-methyl naphthalene, processing step is as follows:
After A, mixed methylnaphthalene cut the naphthalene cut from normal pressure primary distillation tower (1) cat head, liquid directly entered vacuum flash device (2) and separates under keeping warm mode at the bottom of the tower;
B, from vacuum flash device (2) bottom extraction mixed methylnaphthalene, from vacuum flash device (2) cat head extraction 2-methylnaphthalene;
C, enter negative pressure rectifying column (3) from vacuum flash device (2) cat head extraction 2-methylnaphthalene, carry out negative pressure rectifying, the extraction mixed methylnaphthalene enters the raw material tank reuse at the bottom of negative pressure rectifying column (3) tower, from negative pressure rectifying column (3) cat head extraction 2-methyl naphthalene.
In the present embodiment, the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 225 ℃, and reflux ratio is 15.The vacuum of negative pressure rectifying column (3) tower top pressure is 80%, and tower top temperature is 170 ℃, and reflux ratio is 15.
The processing step of present embodiment is identical with embodiment 1, and the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 215 ℃, and reflux ratio is 10.The vacuum of negative pressure rectifying column (3) tower top pressure is 90%, and tower top temperature is 160 ℃, and reflux ratio is 15.
The processing step of present embodiment is identical with embodiment 2, and the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 220 ℃, and reflux ratio is 12.The vacuum of negative pressure rectifying column (3) tower top pressure is 85%, and tower top temperature is 155 ℃, and reflux ratio is 13.
The processing step of present embodiment is identical with embodiment 1, and the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 225 ℃, and reflux ratio is 10.The vacuum of negative pressure rectifying column (3) tower top pressure is 80%, and tower top temperature is 160 ℃, and reflux ratio is 15.
Embodiment 6
The processing step of present embodiment is identical with embodiment 1, and the tower top pressure of normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 215 ℃ ℃, and reflux ratio is 15.The vacuum of negative pressure rectifying column (3) tower top pressure is 85%, and tower top temperature is 170 ℃, and reflux ratio is 10.
Claims (6)
1. the direct distil process of a 2-methyl naphthalene is characterized in that it comprises following processing step:
After A, mixed methylnaphthalene cut the naphthalene cut from normal pressure primary distillation tower (1) cat head, liquid directly entered vacuum flash device (2) and separates under keeping warm mode at the bottom of the tower;
B, from vacuum flash device (2) bottom extraction mixed methylnaphthalene, from vacuum flash device (2) cat head extraction 2-methylnaphthalene;
C, enter negative pressure rectifying column (3) from vacuum flash device (2) cat head extraction 2-methylnaphthalene, carry out negative pressure rectifying, extraction mixed methylnaphthalene at the bottom of negative pressure rectifying column (3) tower is from negative pressure rectifying column (3) cat head extraction 2-methyl naphthalene.
2. the direct distil process of 2-methyl naphthalene according to claim 1 is characterized in that: among the described step C at the bottom of negative pressure rectifying column (3) tower extraction mixed methylnaphthalene enter the raw material tank reuse.
3. the direct distil process of 2-methyl naphthalene according to claim 1 is characterized in that: the tower top pressure of described normal pressure primary distillation tower (1) is a normal pressure, and tower top temperature is 215 ℃～225 ℃, and reflux ratio is 10～15.
4. the direct distil process of 2-methyl naphthalene according to claim 1 is characterized in that: the vacuum of described negative pressure rectifying column (3) tower top pressure is 80～90%, and tower top temperature is 150 ℃～170 ℃, and reflux ratio is 10～15.
5. the direct distil process of 2-methyl naphthalene according to claim 1, it is characterized in that: enter catalyst converter (4) from negative pressure rectifying column (3) cat head extraction 2-methyl naphthalene among the described step C, allow the micro constitutent catalytic polymerization, and by the discharge of catalyst converter (4) bottom, enter separator (5) from the 2-methyl naphthalene of catalyst converter (4) top extraction, isolate the 2-methyl naphthalene.
6. the direct distil process of 2-methyl naphthalene according to claim 5 is characterized in that: described discharge liquid of discharging from catalyst converter (4) bottom enters factory's incinerator or heat-conducting oil furnace burns.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910227226 CN102078699B (en) | 2009-12-01 | 2009-12-01 | Direct distillation technology for 2-methylnaphthalene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910227226 CN102078699B (en) | 2009-12-01 | 2009-12-01 | Direct distillation technology for 2-methylnaphthalene |
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| CN102078699A true CN102078699A (en) | 2011-06-01 |
| CN102078699B CN102078699B (en) | 2013-06-05 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316753A (en) * | 2016-08-23 | 2017-01-11 | 吴江市万事达环保溶剂有限公司 | Separation and purification technology of 2-methylnaphthalene |
| CN106938967A (en) * | 2017-02-08 | 2017-07-11 | 兖矿科蓝凯美特化工有限公司 | A kind of rectifier unit and its production method for flashing the snow-white refined naphthalene of production that decolourizes |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050245763A1 (en) * | 2004-04-29 | 2005-11-03 | Lg Chem, Ltd. | Method for recovering acrylic acid |
| JP2006000787A (en) * | 2004-06-18 | 2006-01-05 | Toshiba Plant Systems & Services Corp | Distillation method and system for polystyrene degraded and produced oil |
| CN1721380A (en) * | 2005-06-30 | 2006-01-18 | 天津大学 | Process for extracting 1-methylnaphthalene and 2-methylnaphthalene from tar |
-
2009
- 2009-12-01 CN CN 200910227226 patent/CN102078699B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050245763A1 (en) * | 2004-04-29 | 2005-11-03 | Lg Chem, Ltd. | Method for recovering acrylic acid |
| JP2006000787A (en) * | 2004-06-18 | 2006-01-05 | Toshiba Plant Systems & Services Corp | Distillation method and system for polystyrene degraded and produced oil |
| CN1721380A (en) * | 2005-06-30 | 2006-01-18 | 天津大学 | Process for extracting 1-methylnaphthalene and 2-methylnaphthalene from tar |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106316753A (en) * | 2016-08-23 | 2017-01-11 | 吴江市万事达环保溶剂有限公司 | Separation and purification technology of 2-methylnaphthalene |
| CN106938967A (en) * | 2017-02-08 | 2017-07-11 | 兖矿科蓝凯美特化工有限公司 | A kind of rectifier unit and its production method for flashing the snow-white refined naphthalene of production that decolourizes |
| CN106938967B (en) * | 2017-02-08 | 2023-05-12 | 兖矿科蓝凯美特化工有限公司 | Rectifying device for producing snow white refined naphthalene through flash evaporation and decoloration and production method thereof |
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| CN102078699B (en) | 2013-06-05 |
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