CN100999564A - Process for producting petruleum resin by hot polymerizing - Google Patents
Process for producting petruleum resin by hot polymerizing Download PDFInfo
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- CN100999564A CN100999564A CN 200610130712 CN200610130712A CN100999564A CN 100999564 A CN100999564 A CN 100999564A CN 200610130712 CN200610130712 CN 200610130712 CN 200610130712 A CN200610130712 A CN 200610130712A CN 100999564 A CN100999564 A CN 100999564A
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Abstract
The present invention relates to hot polymerization process of producing petroleum resin, especially with C9 fraction as the side product of ethylene production. The C9 fraction material is first cut into three fraction sections including styrene resin oil, dicyclopentadiene resin oil and indene resin oil; and the three fraction sections are added into hot polymerization reaction kettle according to the requirement of the product for polymerizing, with the hot polymerization reaction kettle comprising four serially connected kettles with separate regulation on temperature, pressure, material retention time and other parameters. The product obtained through polymerization in the four serially connected kettles is distilled to eliminate solvent so as to obtain the petroleum resin product.
Description
Technical field
The present invention relates to a kind of thermopolymerization and produce the method for petroleum resin, be specially adapted to the thermopolymerization of ethylene by-product C9 cut and produce petroleum resin.
Background technology
The C9 cut is one of main by product of producing by ethene, can be used for producing important Chemicals petroleum resin.The method of utilizing the C9 fraction to produce petroleum resin at present mainly contains two kinds, and a kind of is positively charged ion catalytic low temperature polymerization method (being called for short cold poly-method), and another kind is to add thermal initiation radical polymerization (abbreviation thermal polymerization method).
It is to utilize dicyclopentadiene in the cracking of ethylene C9 cut, vinyl toluene isoreactivity component under heating condition that thermal polymerization method is produced the C9 Petroleum Resin Synthesized with Thermal Polymerization, the sintetics by radical polymerization.The C9 Petroleum Resin Synthesized with Thermal Polymerization has good affinity, thermostability and good solubility, is widely used in industries such as paint, printing ink, tackiness agent, rubber.The major advantage of thermal polymerization method is that production process is not used catalyzer, thereby can not produce a large amount of harmful waste waters because of handling catalyzer.But because cracking of ethylene C9 fractions consisting is very complicated, the C9 petroleum resin are produced in thermopolymerization, and the colourity of product, softening temperature etc. are very unstable.
CN 1027541C adopts cracking of ethylene C9 cut, adds peroxide initiator, and after distillation cut out 140 ℃～240 ℃ cut, still is residual to be distilled under vacuum to 220 ℃～280 ℃, obtains dark Petroleum Resin Synthesized with Thermal Polymerization.This invention can only obtain dark Petroleum Resin Synthesized with Thermal Polymerization owing to can not control temperature, the pressure of thermopolymerization different steps according to reaction mechanism.
CN 1356346A is that to be rich in the cut of unsaturated olefin one or more be raw material to C9 cut, C 5 fraction, dicyclopentadiene cut with petroleum cracking system ethylene by-product etc., polyreaction under 170 ℃～280 ℃ and 0.3～3.5MPa condition, do not add or add less initiator, distillation is removed low cut and is obtained petroleum resin.This invention is by adding C 5 fraction, and the range of molecular weight distributions of having dwindled product still still can not solve the dark problem of product colourity.
Because prior art is controlled polymerization progress, polymerization temperature well, thereby can not control the colourity and the softening temperature of hot polymerization petroleum resin well, Ji Shi (Gardner) colourity is generally greater than 12
#, the softening temperature distribution range is also bigger, makes the range of application of hot polymerization petroleum resin products be affected.In addition, when prior art adopted common distillation method to remove unpolymerized solvent composition, because still temperature is high, material viscosity was big, easy local buildup, and generation stain and coking have a strong impact on the quality and the colourity of product.
Summary of the invention
The present invention is intended to overcome the deficiencies in the prior art, the method that provides a kind of new thermopolymerization to produce petroleum resin.
The object of the present invention is achieved like this: the method for petroleum resin is produced in a kind of thermopolymerization, it is characterized in that: at first the C9 raw material is separated into styrene resin oil, dicyclopentadiene resinoid oil, three parts of indenes resinoid oil, again the material of three parts is fed four thermopolymerization stills that are cascaded simultaneously continuously, carry out heat polymerization, material afterwards removes solvent through falling film evaporation, and cooling granulation obtains petroleum resin products.
We find, various components in the C9 cut, have only wherein styrenic, dicyclopentadiene class, the thermopolymerization at high temperature of indenes class isoreactivity component to generate petroleum resin, components such as all the other alkyl benzenes, condensed-nuclei aromatics class can not thermopolymerization, can only play the effect of solvent.A complete heat polymerization process is made up of three phases, and the initial stage of thermopolymerization is swift in response, and heat release is violent, easy local superheating, and colourity deepens, and this stage generates a large amount of small molecules polymkeric substance; The mid-term stage of thermopolymerization, speed of response descends, and heat release is stable, and this stage small molecules polymkeric substance begins to grow up; The later stage of thermopolymerization, speed of response is slow, and heat release reduces rapidly, and this stage polymer molecule continues to grow up.The technology in past, heat polymerization is to occur in the same still, under the situation of continuously feeding and discharging, has the heat polymerization of three different stepss in the same still simultaneously, therefore be difficult to avoid local superheating, also be difficult to the width of controlling polymers molecular weight distribution.In view of the above, the present invention has designed four stills series connection heat polymerization technology, effectively separately the material that is in the differential responses stage, in view of the factors such as temperature of reaction, pressure and the residence time of each step of reaction all influential to the colourity and the softening temperature that generate resin, processing condition such as temperature of reaction that just can be by adjusting single still, pressure, the residence time are produced the product of different qualities.Particularly, dicyclopentadiene resinoid oil is directly fed the still that is arranged in four series connection thermopolymerization stills than the back, can effectively reduce product softening temperature and colourity.Adopt the secondary falling-film evaporator to remove the solvent in the material behind the heat polymerization, be according to the material characteristics that viscosity increases along with solvent removal, in the lower temperature of the 1st grade of falling-film evaporator, the 2nd grade of falling-film evaporator is with higher temperature, thereby material is under the same comparatively high temps all the time, and the liquid film that material forms in falling-film evaporator is evenly smooth, can not produce buildup, local superheating and dead angle.
It is standby that the present invention program at first obtains C9 raw material rectifying cutting higher three the cut sections of indenes resinoid oil of medium dicyclopentadiene resinoid oil of boiling point lower styrene resin oil, boiling point and boiling point successively.The thermopolymerization still is four stirring tank series connection, and each thermopolymerization still is operating parameterss such as attemperation, pressure, residence time of material separately.So just be equivalent to heat polymerization process is divided into four step of reaction, carry out the initial stage of heat polymerization in the 1st thermopolymerization still, carry out the later stage of heat polymerization in the mid-term stage that carries out thermopolymerization in the 2nd and the 3rd the thermopolymerization still, the 4th thermopolymerization still.According to the characteristics of each step of reaction, control temperature, the pressure of each thermopolymerization still respectively, just can control the molecular weight distribution and the colourity of heat polymerization product.In three cut sections that C9 rectifying obtains, styrene resin oil and indenes resinoid oil is the 1st thermopolymerization still of feeding continuously simultaneously, and dicyclopentadiene resinoid oil can feed in four thermopolymerization stills any one continuously.When continuous production, it is more to produce heat in the 1st still, needs suitably to take out reaction heat, and heat is in a basic balance in the 2nd and the 3rd still, then needs suitably to import heat in the 4th still.In order to guarantee that heat polymerization steadily carries out, the still of general back has higher temperature and pressure than the still of front.Such design is highly beneficial, such as, obtain softening temperature and colourity high product, can increase temperature, pressure and the residence time of each thermopolymerization still; Obtain the lower product of softening temperature and colourity, can reduce temperature, pressure and the residence time of each thermopolymerization still.Particularly, dicyclopentadiene resinoid oil feeds the thermopolymerization still than the front, can obtain softening temperature and colourity high product; Dicyclopentadiene resinoid oil feeds the thermopolymerization still than the back, can obtain the lower product of softening temperature and colourity.Material behind the four stills series connection hot polymerization, process secondary falling-film evaporator removes solvent wherein again, and cooling is granulated and is promptly obtained petroleum resin products.
Four stills series connection heat polymerization, wherein the 1st thermopolymerization still temperature of reaction is 210 ℃～240 ℃, pressure 0.2MPa～0.5MPa, residence time 4h～6h, 220 ℃～250 ℃ of the 2nd thermopolymerization still temperature of reaction, pressure 0.5MPa～1.0MPa, residence time 4h～6h, 230 ℃～260 ℃ of the 3rd thermopolymerization still temperature of reaction, pressure 0.8MPa～1.5MPa, residence time 4h～6h, 230 ℃～280 ℃ of the 4th thermopolymerization still temperature of reaction, pressure 1.0MPa～2.1MPa, residence time 4h～6h.Products obtained therefrom is measured according to GB/T2294 petroleum resin softening point measurement method (ring and ball method), and 80 ℃～130 ℃ of softening temperatures are measured colourity 7 according to Ji Shi (Gardner) colorimetry
#～14
#
The softening temperature that Petroleum Resin Synthesized with Thermal Polymerization product of the present invention reaches, chromaticity index tabulation 1.
Softening temperature, chromaticity index that table 1 product of the present invention reaches
| Project | Quality index | ||||
| The softening temperature trade mark | PR-90 | PR-100 | PR-110 | PR-120 | PR-130 |
| Softening point range (ring and ball method) | 80-90 | 90-100 | 100-110 | 110-120 | 120-130 |
| Look number (GShi colorimetry) | 7 #-10 # | 9 #-11 # | 10 #-12 # | 11 #-13 # | 12 #-14 # |
Heat polymerization can be as required, adds initiator in four thermopolymerization stills 1 or several, and initiator can be with superoxide or sodium soap.
The secondary falling-film evaporator can atmospheric operation, also can decompression operation.115 ℃～170 ℃ of falling-film evaporator 1 service temperatures, pressure 0.03MPa～normal pressure, 125 ℃～190 ℃ of falling-film evaporator 2 service temperatures, pressure 0.03MPa～normal pressure.
The invention has the advantages that, produce petroleum resin with four stills series connection carrying out C9 thermopolymerization, overcome traditional single still reaction and can not control the shortcoming of thermopolymerization process and product softening temperature, colourity flexibly, operating parameterss such as the temperature by regulating single heat polymerization still, pressure, the residence time, select the different feed location of dicyclopentadiene resinoid oil, just can control the indexs such as softening temperature, colourity of the process of hot polymerization reaction and petroleum resin products, solve the difficult point that thermal polymerization method can not be produced low colourity petroleum resin; Adopt the secondary falling-film evaporator to remove solvent, solved problems such as stain that common distillation desolventizing can run into, coking effectively.
Description of drawings
Fig. 1 is device of the present invention and schematic flow sheet.Among the figure: the 1st, C9 raw material separating rectification tower, the 2nd, styrene resin oil supply tank, the 3rd, indenes resinoid oil supply tank, the 4th, dicyclopentadiene resinoid oil supply tank, the 5th, thermopolymerization still 1,6th, thermopolymerization still 2,7th, thermopolymerization still 3, the 8th, thermopolymerization still 4,9th, falling-film evaporator 1,10th, falling-film evaporator 2. is a valve,
Be pump.
Embodiment
Following examples are used for further specifying content of the present invention, do not limit application of the present invention.All operations among the embodiment all is to carry out continuously.
Referring to accompanying drawing 1, at first, in styrene resin oil supply tank (2), collect 104 ℃～115 ℃ cuts the rectifying cutting under 0.03MPa in C9 raw material separating rectification tower (1) of C9 raw material, obtain styrene resin oil (hereinafter to be referred as I); In dicyclopentadiene resinoid oil supply tank (4), collect 115 ℃～118 ℃ cuts, obtain dicyclopentadiene resinoid oil (hereinafter to be referred as II); In indenes resinoid oil supply tank (3), collect 118 ℃～121 ℃ cuts, obtain indenes resinoid oil (hereinafter to be referred as III), obtain three cut sections altogether.
Embodiment 1
Referring to accompanying drawing 1, I, II, III that the distillation of C9 raw material is obtained feed thermopolymerization still 1 (5), 240 ℃ of control reactor 1 temperature, pressure 0.5MPa, residence time 6h; Material in the thermopolymerization still 1 enters thermopolymerization still 2 (6), 250 ℃ of control thermopolymerization still 2 temperature, pressure 1.0MPa, residence time 6h; Material in the thermopolymerization still 2 enters thermopolymerization still 3
(7), 260 ℃ of control thermopolymerization still 3 temperature, pressure 1.5MPa, residence time 6h; Material in the thermopolymerization still 3 enters thermopolymerization still 4 (8), 280 ℃ of control thermopolymerization still 4 temperature, pressure 2.1MPa, residence time 6h.The material that comes out from thermopolymerization still 4 enters the secondary falling-film evaporator, 170 ℃ of falling-film evaporator 1 (9) temperature, and pressure is normal pressure, 190 ℃ of falling-film evaporator 2 (10) temperature, pressure is normal pressure, removes the granulation of solvent postcooling, obtain 130 ℃ of product softening temperatures, Ji Shi colourity 14
#
Embodiment 2
Referring to accompanying drawing 1, I, IH are fed thermopolymerization still 1 (5), II feeds thermopolymerization still 4 (6), 210 ℃ of control thermopolymerization still 1 temperature, pressure 0.2MPa, residence time 4h; Material in the thermopolymerization still 1 enters thermopolymerization still 2 (6), 220 ℃ of control thermopolymerization still 2 temperature, pressure 0.5MPa, residence time 4h; Material in the thermopolymerization still 2 enters thermopolymerization still 3
(7), 230 ℃ of control thermopolymerization still 3 temperature, pressure 0.8MPa, residence time 4h; Material in the thermopolymerization still 3 enters thermopolymerization still 4 (8), 230 ℃ of control thermopolymerization still 4 temperature, pressure 1.0MPa, residence time 4h.The material that comes out from thermopolymerization still 4 enters the secondary falling-film evaporator, 115 ℃ of falling-film evaporator 1 (9) temperature, pressure 0.03MPa, 125 ℃ of falling-film evaporator 2 (10) temperature, pressure 0.03MPa removes the granulation of solvent postcooling, obtain 80 ℃ of product softening temperatures, Ji Shi colourity 7
#
Embodiment 3
Referring to accompanying drawing 1, I, III are fed thermopolymerization still 1 (5), and the Peracetic Acid that adds material quantity 0.01% in thermopolymerization still 1 is as initiator, II feeds thermopolymerization still 3 (7), 230 ℃ of control thermopolymerization still 1 temperature, pressure 0.3MPa, residence time 5h; Material in the thermopolymerization still 1 enters thermopolymerization still 2 (6), 240 ℃ of control thermopolymerization still 2 temperature, pressure 0.8MPa, residence time 5h; Material in the thermopolymerization still 2 enters thermopolymerization still 3 (7), 250 ℃ of control thermopolymerization still 3 temperature, pressure 1.2MPa, residence time 5h; Material in the thermopolymerization still 3 enters thermopolymerization still 4 (8), 250 ℃ of control thermopolymerization still 4 temperature, pressure 1.5MPa, residence time 5h.The material that comes out from thermopolymerization still 4 enters the secondary falling-film evaporator, 155 ℃ of falling-film evaporator 1 (9) temperature, pressure 0.07MPa, 175 ℃ of falling-film evaporator 2 (10) temperature, pressure 0.07MPa removes the granulation of solvent postcooling, obtain 100 ℃ of product softening temperatures, Ji Shi colourity 11
#
Claims (10)
- The method of petroleum resin is produced in 1 one kinds of thermopolymerizations, it is characterized in that: at first the C9 raw material is separated into styrene resin oil, dicyclopentadiene resinoid oil, three parts of indenes resinoid oil, again the material of three parts is fed four thermopolymerization stills that are cascaded simultaneously continuously, carry out heat polymerization, material afterwards removes solvent through falling film evaporation, and cooling granulation obtains petroleum resin products.
- The method that petroleum resin are produced in 2 thermopolymerizations according to claim 1 is characterized in that: described styrene resin oil, indenes resinoid oil feed thermopolymerization still 1, and dicyclopentadiene resinoid oil can feed any one in four thermopolymerization stills respectively.
- The method of petroleum resin is produced in 3 thermopolymerizations according to claim 1, it is characterized in that: wherein the 1st thermopolymerization still temperature of reaction is 210 ℃～240 ℃, pressure 0.2MPa～0.5MPa, 4～6 hours residence time.
- 4, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: 220 ℃～250 ℃ of the 2nd thermopolymerization still temperature of reaction, pressure 0.5MPa～1.0MPa, 4～6 hours residence time.
- 5, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: 230 ℃～260 ℃ of the 3rd thermopolymerization still temperature of reaction, pressure 0.8MPa～1.5MPa, 4～6 hours residence time.
- 6, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: 230 ℃～280 ℃ of the 4th thermopolymerization still temperature of reaction, pressure 1.0MPa～2.1MPa, residence time 4h～6h.
- 7, the method for petroleum resin is produced in thermopolymerization according to claim 1, and it is characterized in that: falling-film evaporator is made as two-stage tandem.
- 8, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: 115 ℃～170 ℃ of falling-film evaporator 1 service temperatures, pressure 0.03MPa～normal pressure.
- 9, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: 125 ℃～190 ℃ of falling-film evaporator 2 service temperatures, pressure 0.03MPa～normal pressure.
- 10, the method for petroleum resin is produced in thermopolymerization according to claim 1, it is characterized in that: add initiator in described four thermopolymerization stills 1 or several.
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| CNB2006101307120A CN100500718C (en) | 2006-12-30 | 2006-12-30 | Process for producing petroleum resin by hot polymerization |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102382261A (en) * | 2011-08-22 | 2012-03-21 | 天津市兴源化工有限公司 | Preparation method for light-chroma aromatic petroleum resin |
| CN102675030A (en) * | 2012-04-18 | 2012-09-19 | 天津大学 | Process method for directly separating petroleum resin raw materials from cracking C9 fraction |
| CN105254810A (en) * | 2015-11-10 | 2016-01-20 | 天津大学 | Continuous production method for petroleum resin |
| CN105294380A (en) * | 2015-11-30 | 2016-02-03 | 天津天大天海化工新技术有限公司 | Method for separation cyclopentadiene and methyl cyclopentadiene from ethylene byproduct C9 and co-production of petroleum resin |
| CN107177022A (en) * | 2017-07-07 | 2017-09-19 | 常州市天鑫新材料科技有限公司 | A kind of diolefin thermal polymerization method prepares the method that the method and mixing carbon nine thermal polymerization method of Petropols produce Petropols |
| CN108219068A (en) * | 2018-01-10 | 2018-06-29 | 安徽同心化工有限公司 | Controllable high-performance polymer resin of a kind of melt viscosity and preparation method thereof |
| CN108752528A (en) * | 2018-06-25 | 2018-11-06 | 安徽同心化工有限公司 | A kind of C9 hot polymerizations resin and its controllable preparation process of molecular weight and softening point |
-
2006
- 2006-12-30 CN CNB2006101307120A patent/CN100500718C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102382261A (en) * | 2011-08-22 | 2012-03-21 | 天津市兴源化工有限公司 | Preparation method for light-chroma aromatic petroleum resin |
| CN102382261B (en) * | 2011-08-22 | 2013-03-06 | 天津市兴源化工有限公司 | Preparation method for light-chroma aromatic petroleum resin |
| CN102675030A (en) * | 2012-04-18 | 2012-09-19 | 天津大学 | Process method for directly separating petroleum resin raw materials from cracking C9 fraction |
| CN102675030B (en) * | 2012-04-18 | 2015-01-07 | 天津大学 | Process method for directly separating petroleum resin raw materials from cracking C9 fraction |
| CN105254810A (en) * | 2015-11-10 | 2016-01-20 | 天津大学 | Continuous production method for petroleum resin |
| CN105294380A (en) * | 2015-11-30 | 2016-02-03 | 天津天大天海化工新技术有限公司 | Method for separation cyclopentadiene and methyl cyclopentadiene from ethylene byproduct C9 and co-production of petroleum resin |
| CN107177022A (en) * | 2017-07-07 | 2017-09-19 | 常州市天鑫新材料科技有限公司 | A kind of diolefin thermal polymerization method prepares the method that the method and mixing carbon nine thermal polymerization method of Petropols produce Petropols |
| CN108219068A (en) * | 2018-01-10 | 2018-06-29 | 安徽同心化工有限公司 | Controllable high-performance polymer resin of a kind of melt viscosity and preparation method thereof |
| CN108219068B (en) * | 2018-01-10 | 2024-04-05 | 安徽同心新材料科技有限公司 | High-performance polymer resin with controllable melt viscosity and preparation method thereof |
| CN108752528A (en) * | 2018-06-25 | 2018-11-06 | 安徽同心化工有限公司 | A kind of C9 hot polymerizations resin and its controllable preparation process of molecular weight and softening point |
| CN108752528B (en) * | 2018-06-25 | 2020-11-20 | 安徽同心新材料科技有限公司 | C9 heat polymerization resin and preparation process with controllable molecular weight and softening point thereof |
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Application publication date: 20070718 Assignee: Fushun Qilong Chemical Co.,Ltd. Assignor: Shandong Qilong chemical Limited by Share Ltd|Tianjin Tianda Tianhai Chemical New Technology Co Ltd Contract record no.: 2012210000119 Denomination of invention: Process for producting petruleum resin by hot polymerizing Granted publication date: 20090617 License type: Exclusive License Record date: 20120913 |
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