CN101723793B - Device and method for separating rough styrene contained in pyrolysis gasoline - Google Patents
Device and method for separating rough styrene contained in pyrolysis gasoline Download PDFInfo
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- CN101723793B CN101723793B CN 200910234363 CN200910234363A CN101723793B CN 101723793 B CN101723793 B CN 101723793B CN 200910234363 CN200910234363 CN 200910234363 CN 200910234363 A CN200910234363 A CN 200910234363A CN 101723793 B CN101723793 B CN 101723793B
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- partition wall
- crude styrene
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- separating
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- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 title claims abstract description 120
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title claims description 14
- 238000005192 partition Methods 0.000 claims abstract description 73
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 238000007599 discharging Methods 0.000 claims abstract description 20
- 238000000605 extraction Methods 0.000 claims description 19
- 238000005336 cracking Methods 0.000 claims description 17
- 239000000470 constituent Substances 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 2
- 239000000203 mixture Substances 0.000 description 8
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 210000000540 fraction c Anatomy 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000004793 Polystyrene Substances 0.000 description 1
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical compound CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000008521 reorganization Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 229920003048 styrene butadiene rubber Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention relates to a device for separating rough styrene contained in pyrolysis gasoline, comprising a rectifying tower, partition walls (7, 8), a liquid distributor, a condenser, a tower-top product buffer tank, liquid collectors (15, 16) and a reboiler, wherein the two partition walls (7, 8) divides the rectifying tower into six parts, i.e. a public rectifying area, a feeding area, a C6-C7 discharging area, a steam stripping area, a rough styrene discharging area and a public stripping area; a partition wall segment is from the top end of the partition wall (7) to the bottom end of the partition wall (8); the top of the public rectifying area is provided with a temperature measuring instrument, and light component C5 fractions are extracted in the public rectifying area; the left side of the partition wall (7) is provided with the feeding area, materials enter from the feeding area, the right side of the partition wall (7) is provided with the C6-C7 discharging area, and the C6-C7 fractions are extracted in the C6-C7 discharging area; the left side of the partition wall (8) is provided with the steam stripping area, and the right side of the partition wall (8) is provided with the rough styrene discharging area; heavy component C9 fractions are extracted in the bottom of the public stripping area, and the bottom of the public stripping area is also provided with the temperature measuring instrument. The invention saves two towers and corresponding accessory equipment due to the rectifying tower with the partition walls (7, 8) and saves the energy by more than 30 percent.
Description
Technical field
The invention belongs to the petrochemical technology field, relate in particular to the apparatus and method of crude styrene in a kind of separating and cracking gasoline.
Background technology
Vinylbenzene is the important monomer of producing polystyrene, ABS resin and styrene-butadiene rubber(SBR).The vinylbenzene that contains about 4%-6% in the pyrolysis gasoline of cracking ethylene factory.In recent years, it is more and more that ethylene unit throughput newly-built or reorganization and expansion reaches the above enterprise of 800kt/a, and the production capacity of raw pyrolysis gasoline is increasing.Traditional working method is to pyrolysis gasoline C
6-C
8cut carries out two-stage hydrogenation, and wherein vinylbenzene is saturated to ethylbenzene, and this not only causes the ethylbenzene concentration in xylol too high, can not be used as isomery level dimethylbenzene, but also waste a large amount of hydrogen resources.
Along with the continuous progress of technology, reclaiming vinylbenzene from raw pyrolysis gasoline has become possibility.By bringing Selection In property solvent, can greatly change the relative volatility of each component, adopt extraction and distillation technology, can be optionally from thick C
8reclaim vinylbenzene in cut.Therefore, reclaim high value added product vinylbenzene from raw pyrolysis gasoline, not only can reduce the ethylbenzene concentration in xylol, dimethylbenzene is appreciated for the isomery level from grade solvent, and significantly the hydrogenation of alleviator is loaded, and reduces the hydrogen consumption.
China Patent Publication No. CN200610029973.3, the patent of invention that name is called the method for purifying styrene " reclaim " discloses with double-column process separates crude styrene.Pyrolysis gasoline is successively through de-C
7tower, de-C
9tower, de-C
9column overhead extraction C
8cut, the C of rich in styrene
8cut is made with extra care to obtain vinylbenzene, its weak point: C
5cut is not effectively separated.C
8cut has carried out twice heating, easily polymerization, thus lose active ingredient vinylbenzene wherein.
At present, in traditional pyrolysis gasoline, the vinylbenzene disjunctive path is as shown in Figure of description 1: pyrolysis gasoline is from the middle part charging of lightness-removing column, removed overhead C
5-C
7, then, at the bottom of its tower, heavy constituent enters the middle part continuation separation of weight-removing column, finally from its tower top outlet, obtain crude styrene, enter downstream crude styrene rectification flow, its weak point: separation process is long, energy consumption is large, the easy polymerization of heat-sensitive substance vinylbenzene, and useful component C
5cut is not effectively separated.
Summary of the invention
It is long that the present invention has overcome in prior art separation process, and energy consumption is large, and useful component C
5cut is not effectively separated, C
8cut carries out twice heating, the easy shortcoming of polymerization, provide the apparatus and method of crude styrene in a kind of separating and cracking gasoline, adopts single tower to separate crude styrene and replaced two tower flow processs of the prior art, with the effect that reaches energy-conservation, reduces investment outlay, obtain useful component C simultaneously
5.
Technical scheme of the present invention is as follows, and in a kind of separating and cracking gasoline, the device of crude styrene, comprise rectifying tower, partition wall 7,8, liquid dispenser 10, condenser 11, overhead product surge tank 12, liquid header 15,16, reboiler 18, wherein two partition walls 7,8 are divided into 6 parts by rectifying tower, i.e. public rectification zone 1, intake zone 2, C
6-C
7discharge zone 3, stripping zone 4, crude styrene discharge zone 5 and public stripping zone 6.Partition wall 7 tops are the partition wall section to partition wall 8 bottoms, and the partition wall section is separated wall 7 and partition wall 8 is divided at least Si Ge district, more than the partition wall section, are wherein public rectification zone 1, below the partition wall section, are public stripping zones 6; Public rectification zone 1 top is provided with temperature measuring set, at this part extraction light constituent C
5cut; The left side of partition wall 7 is intake zone 2, and raw material enters from this part, and right side is C
6-C
7discharge zone 3, from this part of extraction C
6-C
7cut; The left side of partition wall 8 is stripping zones 4, and right side is crude styrene discharge zone 5, from this part of extraction crude styrene cut; Public stripping zone 6 bottom extraction heavy constituent C
9cut, its bottom also is provided with temperature measuring set.
Wherein said rectifying tower can be that packing tower can be also tray column;
Wherein said C
6-C
7the discharging position of cut can be with the feed entrance point of pyrolysis gasoline in the same level position, also can set low 3-7 piece theoretical stage than the feed position of pyrolysis gasoline, described crude styrene discharging position also can set low 3-8 piece theoretical stage than the centre bit of crude styrene discharge zone 5;
Wherein said public rectification zone 1 and public stripping zone 6 have respectively the 5-20% of premier's opinion stage number of dividing wall column; Partition wall 7 is positioned at the middle and upper part of rectifying tower, intake zone 2 and C
6-C
7discharge zone 3 has the 40-60% of premier's opinion stage number of dividing wall column; Partition wall 8 be positioned at partition wall 7 below, the top of partition wall 8 extends into C
6-C
7the about 2-4 piece of discharge zone 3 theoretical stage, the 2-30% that the level interval between partition wall 7 and partition wall 8 is the dividing wall column radius, stripping zone 4 and crude styrene discharge zone 5 have the 15-30% of premier's opinion stage number of dividing wall column.
Method based on the device of crude styrene in above-mentioned a kind of separating and cracking gasoline: raw material enters from the intake zone 2 in the left side of upper partition wall 7, from right side, is C
6-C
7discharge zone 3 extraction C
6-C
7cut, by regulating reflux ratio, wherein said reflux ratio 1-6, control tower top temperature extraction light constituent C in 10-30 ℃ of scope by the temperature measuring set at public rectification zone 1 top
5cut; Regulate and enter C by liquid dispenser 10
6-C
7the quantity of steam that the liquid flow rate of discharge zone 3 or adjusting tower reactor rise, control drop temperature extraction C in 70-90 ℃ of scope
6-C
7cut; The left side of partition wall 8 is stripping zones 4, and right side is crude styrene discharge zone 5, under the condition that guarantees the tower reactor liquid level stabilizing, regulate the load of crude styrene, and drop temperature changes in 90-130 ℃ of scope.Public stripping zone 6 bottoms are provided with temperature measuring set, control column bottom temperature extraction heavy constituent C in 130-160 ℃ of scope
9cut.
The wherein said liquid refluxed from public rectification zone 1 enters liquid header 15, then by liquid dispenser 10, is dispensed to intake zone 2 and C
6-C
7discharge zone 3.The liquid partition ratio is intake zone 2 and C
6-C
7the liquid partition ratio that discharge zone 3 is is 4: 1-1: 4, preferably 2: 1-1: 2.The liquid that liquid header 16 is collected enters crude styrene discharge zone 5.
The working pressure of wherein said rectifying tower is normal pressure or negative pressure, and pressure range is 10-101KPa.
Under these processing condition, tower top C
5content can reach 99.5%, side line C
6-C
7middle C
5content is less than 2%, side line C
6-C
7middle C
8content be less than 1%, C in crude styrene
6-C
7content be less than 1%, cinnamic yield can reach more than 99%, tower reactor C
8content is less than 1% (more than be all the quality percentage composition).
Each compositing range: C in wherein said raw material pyrolysis gasoline
5quality percentage composition 5-30%, preferred 10-20%, C
6-C
7quality percentage composition 30-60%, preferred 40-50%, C
8quality percentage composition 10-40%, preferred 15-30%, C
9quality percentage composition 5-35%, preferred 15-30%.
The present invention compares with traditional separate mode, and the partition wall rectifying tower can replace decarburization five towers, decarburization seven towers, and decarburization nine towers, saved two towers and corresponding auxiliary facility, energy-conservation reaching more than 30%.
The accompanying drawing explanation
Fig. 1 tradition crude styrene disjunctive path constructional device figure, wherein 1 is lightness-removing column, and 2 is weight-removing column, and 4,8 is condenser, and 5,9 is the overhead product surge tank, 7,11 is reboiler;
Fig. 2 partition wall rectifying tower separates crude styrene disjunctive path constructional device figure, and wherein 1 is public rectification zone, and 2 is intake zone, and 3 is C
6-C
7discharge zone, 4 is stripping zone, and 5 is the crude styrene discharge zone, and 6 is public stripping zone, and 7 is upper partition wall, and 8 is lower partition wall, and 10 is liquid dispenser, and 11 is condenser, and 12 is the overhead product surge tank, and 15,16 is liquid header, and 18 is reboiler.
Embodiment
The device of crude styrene in a kind of separating and cracking gasoline shown in Fig. 2, wherein two partition walls 7,8 are divided into 6 parts by rectifying tower, i.e. public rectification zone 1, intake zone 2, C
6-C
7discharge zone 3, stripping zone 4, crude styrene discharge zone 5 and public stripping zone 6; The working pressure of rectifying tower is normal pressure or negative pressure, and pressure range is 10-101KPa.Total number of theoretical plate of rectifying tower is the 100-160 piece, the number of theoretical plate of public rectification zone 1 is the 15-40 piece, zone 2 and zone 3 number of theoretical plates separately are the 20-45 piece, zone 4 and zone 5 separately number of theoretical plate be the 15-40 piece, the number of theoretical plate of public stripping zone 6 is the 10-30 piece.The liquid refluxed from public rectification zone 1 enters liquid header 15, and the liquid that liquid header 15 is collected is dispensed to intake zone 2 and C by liquid dispenser 10
6-C
7discharge zone 3, the liquid that liquid header 16 is collected enters crude styrene discharge zone 5.Raw material enters the central zone of intake zone 2, light constituent C
5enter public rectification zone, C
6-C
7cut freely separates at the two ends of partition wall 7, and heavy constituent enters stripping zone 4, light constituent C
5complete the process of purification in public rectification zone, pure fraction C
5discharge C from tower top
6-C
7cut 3 carries out concentrate in zone, and at the central zone extraction C in zone 3
6-C
7cut.C
8cut freely separates at the two ends of partition wall 8, thereby, the central zone extraction crude styrene of crude styrene discharge zone, high boiling fraction C
9from tower reactor, discharge.
With the charging of table 1 raw material, partition wall rectifying tower height H=8300mm, diameter 76mm, the high 2500mm of partition wall 7, the high 1500mm of partition wall 8, premier's opinion stage number is the 100-110 piece, tower top pressure 1atm, the central position charging of intake zone 2, input speed is 10kg/h, reflux ratio is 2, liquid partition ratio (C
6-C
7discharge zone 3: intake zone 2) be 2: 1, tower top discharging 1.5kg/h, C
6-C
7discharge zone 3 central position dischargings, side line C
6-C
7rate of yield is 4.7kg/h, the central position discharging of crude styrene discharge zone 5, side line C
8rate of yield is 2.5kg/h, tower top temperature 15-20 ℃, C
6-C
7drop temperature 80-85 ℃, crude styrene drop temperature 110-120 ℃, tower reactor temperature 150-160 ℃.Tower top C with this understanding
5the quality percentage composition reach 99.50%; Side line C
6-C
7c in discharging
5massfraction be 1.56%; Cinnamic yield can reach 99.04%, tower reactor C
8massfraction be 0.60%.
The massfraction of each component of table 1 pyrolysis gasoline
Embodiment 2
With the charging of table 1 raw material, in the partition wall rectifying tower identical with embodiment 1, in the identical situation of operational condition, only change the discharging position, side line C
6-C
7c is compared in the discharging position
6-C
7the centre bit of discharge zone 3 sets low 5 theoretical stages, and crude styrene discharging position sets low 3 theoretical stages, tower top C with this understanding than the centre bit of crude styrene discharge zone 5
5the quality percentage composition reach 99.90%; Side line C
6-C
7c in discharging
5massfraction be 0.85%; Cinnamic yield can reach 99.20%, tower reactor C
8massfraction be 0.30%
Embodiment 3
The massfraction of each component of table 2 pyrolysis gasoline
With the charging of table 2 raw material, in the partition wall rectifying tower identical with embodiment 1, the input and output material position is identical with embodiment 1, tower top pressure 0.5atm, input speed is 10kg/h, and reflux ratio is 2, liquid partition ratio (C6-C7 discharge zone 3: intake zone 2) be 1: 2, tower top discharging 1.0kg/h, side line C6-C7 rate of yield is 4.7kg/h, and side line C8 rate of yield is 3.0kg/h, C6-C7 drop temperature 60-75 ℃, crude styrene drop temperature 90-100 ℃, tower reactor temperature 130-140 ℃.The quality percentage composition of tower top C5 reaches more than 99.95% with this understanding; In side line C6-C7 discharging, the massfraction of C5 is 0.46%; Cinnamic yield can reach 99.50%, and the massfraction of tower reactor C8 is 0.50%.
Claims (10)
1. the device of crude styrene in a separating and cracking gasoline, comprise rectifying tower, the first partition wall (7), the second partition wall (8), liquid dispenser (10), condenser (11), overhead product surge tank (12), liquid header (15,16), reboiler (18), it is characterized in that the first partition wall (7) and the second partition wall (8) are divided into 6 parts by rectifying tower, be public rectification zone (1), intake zone (2), C
6-C
7discharge zone (3), stripping zone (4), crude styrene discharge zone (5) and public stripping zone (6); The first partition wall (7) top to the second partition wall (8) bottom is the partition wall section, the partition wall section is divided into Si Ge district or above interval by the first partition wall (7) and the second partition wall (8), more than the partition wall section, being wherein public rectification zone (1), is public stripping zone (6) below the partition wall section; Extraction light constituent C
5public rectification zone (1) top of cut is provided with temperature measuring set; The left side of the first partition wall (7) is incoming stock intake zone (2), and right side is extraction C
6-C
7the C of cut
6-C
7discharge zone (3); The left side of the second partition wall (8) is stripping zone (4), and right side is crude styrene discharge zone (5); Extraction heavy constituent C
9public stripping zone (6) bottom of cut is provided with temperature measuring set.
2. the device of crude styrene in a kind of separating and cracking gasoline according to claim 1, is characterized in that described rectifying tower is packing tower or tray column.
3. the device of crude styrene in a kind of separating and cracking gasoline according to claim 1, it is characterized in that the first partition wall (7) in described rectifying tower is positioned at the central position of tower, perhaps offset central position left, the cross-sectional area of intake zone (2) is more than or equal to C
6-C
7the cross-sectional area of discharge zone (3), its ratio is 2:1-1:1.
4. the device of crude styrene in a kind of separating and cracking gasoline according to claim 1, is characterized in that described C
6-C
7the discharging position of cut sets low 3-7 piece theoretical stage than the feed position of pyrolysis gasoline, and described crude styrene discharging position sets low 3-8 piece theoretical stage than the centre bit of crude styrene discharge zone (5).
5. the device of crude styrene in a kind of separating and cracking gasoline according to claim 1, is characterized in that described C
6-C
7the discharging position of cut and the feed entrance point of pyrolysis gasoline are in the same level position.
6. the device of crude styrene in a kind of separating and cracking gasoline according to claim 1, is characterized in that described public rectification zone (1) and public stripping zone (6) have respectively the 5-20% of premier's opinion stage number of dividing wall column; The first partition wall (7) is positioned at the middle and upper part of rectifying tower, intake zone (2) and C
6-C
7discharge zone (3) has the 40-60% of premier's opinion stage number of dividing wall column; The second partition wall (8) be positioned at the first partition wall (7) below, the top of the second partition wall (8) extends into C
6-C
72-4 piece theoretical stage in discharge zone (3), the 2-30% that level interval between the first partition wall (7) and the second partition wall (8) is the dividing wall column radius, stripping zone (4) and crude styrene discharge zone (5) have the 15-30% of premier's opinion stage number of dividing wall column.
7. a method of utilizing crude styrene in device separating and cracking gasoline claimed in claim 1: raw material from the intake zone (2) in left side of the first partition wall (7) enter, from right side, be C
6-C
7discharge zone (3) extraction C
6-C
7cut, regulate reflux ratio, and wherein said reflux ratio 1-6 controls tower top temperature extraction light constituent C in 10-30 ℃ of scope by the temperature measuring set at public rectification zone (1) top
5cut; Regulate and enter C by liquid dispenser (10)
6-C
7the quantity of steam that the liquid flow rate of discharge zone (3) or adjusting tower reactor rise, control drop temperature extraction C in 70-90 ℃ of scope
6-C
7cut; The left side of the second partition wall (8) is stripping zone (4), and right side is crude styrene discharge zone (5), regulate the load of crude styrene, and drop temperature is in 90-130 ℃ of scope; Public stripping zone (6) bottom is provided with temperature measuring set, controls column bottom temperature extraction heavy constituent C in 130-160 ℃ of scope
9cut.
8. the method for crude styrene in a kind of separating and cracking gasoline according to claim 7, is characterized in that the liquid refluxed from public rectification zone (1) enters liquid header (15), then is dispensed to intake zone (2) and C by liquid dispenser (10)
6-C
7discharge zone (3); The liquid partition ratio is intake zone (2) and C
6-C
7the liquid partition ratio 4:1-1:4 of discharge zone (3).
9. the method for crude styrene in a kind of separating and cracking gasoline according to claim 8, is characterized in that the liquid partition ratio is intake zone (2) and C
6-C
7the liquid partition ratio of discharge zone (3) is 2:1-1:2.
10. the method for crude styrene in a kind of separating and cracking gasoline according to claim 7, the working pressure scope that it is characterized in that wherein said rectifying tower is 10-101 KPa.
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|---|---|---|---|
| CN 200910234363 CN101723793B (en) | 2009-11-24 | 2009-11-24 | Device and method for separating rough styrene contained in pyrolysis gasoline |
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|---|---|---|---|
| CN 200910234363 CN101723793B (en) | 2009-11-24 | 2009-11-24 | Device and method for separating rough styrene contained in pyrolysis gasoline |
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| CN101723793B true CN101723793B (en) | 2013-12-18 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102732284A (en) * | 2011-04-08 | 2012-10-17 | 新疆独山子天利实业总公司 | Technology for removing colloid from cracking-byproduct carbon ten material |
| CN102631791B (en) * | 2012-03-31 | 2016-03-09 | 中国石油化工股份有限公司 | A kind of control method of rectifying tower with bulkhead |
| CN103664489B (en) * | 2012-09-05 | 2016-04-13 | 中国石油化工股份有限公司 | Produce the rectificating method of para-xylene product |
| CN103360216B (en) * | 2013-08-01 | 2014-11-05 | 万华化学集团股份有限公司 | Device and method for preparing fatty alcohol by carboxylate hydrolysis |
| CN105771295B (en) * | 2016-05-19 | 2017-11-17 | 河北工业大学 | The partitioned column of the component mixture of separation four of controllable vapour phase distribution ratio |
| SG11201913269XA (en) * | 2017-09-28 | 2020-04-29 | Exxonmobil Res & Eng Co | Dual-dividing wall column with multiple products |
| CN113355131B (en) * | 2020-03-05 | 2023-01-06 | 中国石化工程建设有限公司 | Multi-working-condition operation device and method for decarbonization nine towers of pyrolysis gasoline hydrogenation device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
| CN101429088A (en) * | 2007-11-07 | 2009-05-13 | 中国石油化工股份有限公司 | Distillation method for separating ethylbenzene and vinyl benzene-containing flow |
-
2009
- 2009-11-24 CN CN 200910234363 patent/CN101723793B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101348412A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Energy-saving method for phenyl ethylene rectification |
| CN101429088A (en) * | 2007-11-07 | 2009-05-13 | 中国石油化工股份有限公司 | Distillation method for separating ethylbenzene and vinyl benzene-containing flow |
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