CN108329429A - A kind of continuous method for preparing light dicyclopentadiene petroleum resin - Google Patents
A kind of continuous method for preparing light dicyclopentadiene petroleum resin Download PDFInfo
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- CN108329429A CN108329429A CN201810186351.4A CN201810186351A CN108329429A CN 108329429 A CN108329429 A CN 108329429A CN 201810186351 A CN201810186351 A CN 201810186351A CN 108329429 A CN108329429 A CN 108329429A
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F240/00—Copolymers of hydrocarbons and mineral oils, e.g. petroleum resins
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
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- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F8/00—Chemical modification by after-treatment
- C08F8/04—Reduction, e.g. hydrogenation
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Abstract
The present invention relates to a kind of continuous methods for preparing light dicyclopentadiene petroleum resin, include the following steps：Dicyclopentadiene monomer and polymer solvent are continuously entered in polymeric kettle and prepare dicyclopentadiene petroleum resin through thermal polymerization, obtained polymerization liquid directly carries out continuously hydrogen adding.Hydrogenation reaction solution removes solvent through flash distillation, and oligomer is removed into vacuum distillation tower, and finally cooling obtains solid light colour petroleum resin.The method of the present invention shortens technological process, simple equipments, especially with continuous one-pot thermal polymerization, equipment investment cost is reduced, process control operations are simplified, obtained polymerization liquid is directly entered hydrogenation plant, it effectively shortens the production cycle about 20%, reduces energy consumption, increase benefit.
Description
Technical field
The present invention relates to high polymer synthesis field more particularly to a kind of sides preparing light dicyclopentadiene petroleum resin
Method.
Background technology
Dicyclopentadiene petroleum resin is that the purity that by-product when petroleum cracking prepares alkene is isolated to is higher
Dicyclopentadiene is reacted through hot polymerization and is obtained.The resin degree of unsaturation is high, and oxidation stability is bad, should not directly use, by adding
Hydrogen can be such that the double bond in resin is saturated, and obtain light, fast light, the good resin of hot property, can be used as heating adhesive or pressure-sensitive
Adhesive, to expand its application range.
Patent CN101003602 discloses a kind of multi-floating bodies Continuous Heat consor production C9 Petropols techniques, technique master
It includes the pretreatment of nine feed purification of carbon to want step, and multi-floating bodies thermal polymerization, material enters level-one evaporator and arrives two level again after polymerization
Falling liquid film flash vessel, finally slice cooling.
Patent CN102516461 discloses a kind of preparation side of light color and high softening-point hydrogenation dicyclopentadiene petroleum resin
Resin raw material is mainly dissolved in selected solvent by method, this method again, is entered in fixed bed reactors after adsorption tower cleans
Carry out catalytic hydrogenation.Catalyst is special nickel zinc silicon bimetallic catalyst.
Polymeric segment in above-mentioned technology with plus hydrogen section be two sections of independent process, it is more complicated that polymeric segment uses equipment
Multi-floating bodies continuous polymerization technique, polymerization liquid need to remove solvent and oligomer control product softening point, obtain melting basis
Petropols, are re-dissolved in after adding hydrogen solvent and enter hydrogenation technique section, and full-flow process is cumbersome.
Invention content
The technical problem to be solved by the present invention is to a kind of polymerization liquids of present situation offer for the prior art without de-
The method that can be carried out continuously the light dicyclopentadiene petroleum resin of continuous preparation for adding hydrogen except solvent.
Technical solution is used by the present invention solves above-mentioned technical problem：The light dicyclopentadiene oil of the continuous preparation
The method of resin, it is characterised in that include the following steps：
Dicyclopentadiene feedstock and atent solvent are continuously introduced into reaction kettle and carry out thermal polymerization, is controlled in the reaction kettle
Reaction temperature is 220~270 DEG C, 0.5~2.0MPa of reaction pressure, in reaction kettle liquid level in the stop of 60~80%, material
Between 0.5~20.0h；Polymerization liquid is obtained in the outlet of reaction kettle；
The amount for controlling atent solvent described in reaction system in the polymeric kettle is 55~85wt% of reaction raw materials total amount；
The atent solvent is in aromatic hydrocarbon, cycloalkane, linear paraffin, de- aromatic hydrocarbon aliphatic category and isomeric alkane hydro carbons
At least one；
Send to the flash distillation removing of the first flash tank the 0.5~4.0wt% for accounting for raw material monomer not anti-obtained polymerization liquid
After answering monomer, after filtering out colloid and other impurities using 100~400 mesh filter screen filters, into hydrogenation reactor；Described in control
The reaction condition of hydrogenation reactor is：6.0~15.0MPa of reaction pressure, 200~280 DEG C of reaction temperature, volume space velocity 0.3~
1.0h~1, hydrogen-oil ratio 500:1~1000:1；Hydrogenation catalyst is loaded palladium catalyst, and the mass fraction of Pd is 0.5~2.0%,
Catalyst carrier is γ-Al2O3, and specific surface area is 80~250m2/g；
Add the hydrogenation resin liquid obtained after hydrogen to be delivered to the second flash tank and steam solvent, obtains flash distillation resin liquid；Control is dodged
Steam 170~200 DEG C of temperature, 80~200kPa of flashing pressure；
The flash distillation resin liquid is delivered to destilling tower to be evaporated under reduced pressure, it is 180 to control the tower top temperature in destilling tower
~220 DEG C, operating pressure is 10~20kPa, and oligomer is discharged from the tower top of destilling tower, is obtained in the bottom of tower of destilling tower light double
Cyclopentadiene petroleum resin.
Preferably, the dicyclopentadiene feedstock can be petroleum cracking C5 mixtures, in the dicyclopentadiene feedstock
Dicyclopentadiene content is 67~87wt%.
Atent solvent in above-mentioned each scheme can select as needed it is in the prior art any one, it is preferably, described
Atent solvent can be selected from benzene,toluene,xylene, trimethylbenzene, hexane, hexamethylene, heptane, octane, nonane, certain herbaceous plants with big flowers alkane, 11 carbon
In alkane, 12 carbon alkane, No. 100 solvent naphthas, No. 200 solvent naphthas, solvent D40, solvent D60, Isopar H and Isopar L extremely
Few one kind.
Further, the top gas phase outlet of the polymeric kettle can also be sequentially connected condenser and dispenser, described poly-
The gaseous substance in kettle is closed after pipeline introduces condenser condensation, liquid phase and the cyclopentadiene raw material isolated enter static state
After mixer mixing, enter the polymeric kettle from the lower part of the polymeric kettle.
Add hydrogen it is possible to further fill into atent solvent to the polymerization liquid of the polymeric kettle and enter after mixing
Reactor；The amount for filling into atent solvent accounts for 0.5~5.0wt% of polymerization liquid.Further to improve the quality of product.
Compared with prior art, the continuous method for preparing light dicyclopentadiene petroleum resin provided by the present invention, no
Polymeric segment is only reduced to one-pot continuous polymerization, and polymerization liquid can be directly entered continuous add without removing polymer solvent
Hydrogen section simplifies technical operation flow to save de- polymer solvent process procedure, effectively shortens the production cycle about 20%, and
And realization is energy-saving, reduces environmental pollution, and reduces equipment investment cost, simple process, equipment investment is reduced, obtained product
Form and aspect are good.
Description of the drawings
Fig. 1 is the flow diagram of the embodiment of the present invention 1.
Wherein：
1, polymeric kettle；2, condenser；3, dispenser；4,12, static mixer；5,8,11, delivery pump；6, inlet valve；7、
Outlet valve；9,13, heat exchanger；10, the first flash tank；14, hydrogenation reactor；15, the second flash tank；16, destilling tower.
Specific implementation mode
Below in conjunction with attached drawing embodiment, present invention is further described in detail.
Hydrogenation catalyst used in embodiment 1 to embodiment 4 is loaded palladium catalyst, and the mass fraction of Pd is
1.0%, catalyst carrier is γ-Al2O3, specific surface area 220m2/g。
Embodiment 1
As shown in Figure 1, by dicyclopentadiene and trimethylbenzene atent solvent by weight 35:Polymeric kettle 1 is put into after 65 mixing
In, level stability is 70%, when being to slowly warm up to 270 DEG C with the speed of 2~3 DEG C/min, inlet valve and outlet valve is opened, by going out
Expect that the residence time of Liquid level polymerisation raw material in valve opening and kettle is 0.7h.
In the unreacted gas phase reaction raw material of the top gas phase outlet discharge of polymeric kettle, enter condenser 2 via pipeline,
It condenses to after 20~30 DEG C, enters back into dispenser 3, the liquid phase isolated enters static mixer 4 with cyclopentadiene raw material and mixes
Afterwards, by pump 5 polymeric kettle 1 is sent into from the lower part of the polymeric kettle.
It is continuously sent to the first flash tank 10 by pump 8 in the polymerization liquid that polymeric kettle bottom obtains, normal pressure removing accounts for monomer
The unreacted monomer of raw material 1.5wt%, after filtering out colloid and other impurities using 100 mesh filter screen filters, then with pipeline supplement
The atent solvent for accounting for polymerization liquid 2.0wt% together enter static mixer 12 in mixing after, through heat exchanger 13 heat exchange extremely
200 DEG C, continuous conveying is extremely plus in hydrogen decoloring reaction device 14.Hydrogen is catalyzed by entering together with polymerization liquid after compressor boost
Agent bed, control add 250 DEG C, reaction pressure 15MPa, volume space velocity 0.5h of reaction temperature in hydrogen decoloring reaction device 14~1, hydrogen
Oily ratio 600:1.
Reaction solution after hydrogenated decoloration is flashed into the second flash tank 15；Control the sudden strain of a muscle in second flash tank
Steam 200 DEG C of temperature, operating pressure 140kPa.Atent solvent is obtained at the top of the second flash tank, polymerization is pumped to by recycling
Solvent tank is recycled for polymerisation.
Hydrogenation resin liquid is obtained in the bottom of the second flash tank, send to vacuum distillation tower 16 and continues to remove oligomer；Control
200 DEG C of overhead temperature, operating pressure 10kPa；Oligomer is discharged in the tower top of destilling tower, the bottom of tower of destilling tower is melted
Melt resin obtains the light dicyclopentadiene petroleum resin of solid after cooling.It is 112 DEG C, Gardener to test its softening point
Coloration ＜ 1.
Embodiment 2
As shown in Figure 1, by dicyclopentadiene and hexamethylene by weight 25：After 75 mixing in input polymeric kettle 1, liquid level is steady
It is scheduled on 75%, when being to slowly warm up to 260 DEG C with the speed of 2~3 DEG C/min, inlet valve and outlet valve are opened, by discharging valve opening
Residence time with Liquid level polymerisation raw material in kettle is 2.5h.
In the unreacted gas phase reaction raw material of the top gas phase outlet discharge of polymeric kettle, enter condenser via pipeline,
Condensation enters back into dispenser to after 20~30 DEG C, and the liquid phase isolated and cyclopentadiene raw material enter after static mixer mixes,
Enter the polymeric kettle from the lower part of the polymeric kettle.
In the polymerization liquid uninterrupted pumping that polymeric kettle bottom obtains to the first flash tank 10, normal pressure removing accounts for raw material monomer
The unreacted monomer of 1.0wt%, after filtering out colloid and other impurities using 400 mesh filter screen filters, then with pipeline supplement account for
The atent solvent of polymerization liquid 2.0wt% enters together in the second static mixer 12 after mixing, extremely through the heat exchange of heat exchanger 13
100 DEG C, continuous conveying is extremely plus in hydrogen decoloring reaction device 14.Hydrogen is catalyzed by entering together with polymerization liquid after compressor boost
Agent bed, control add 200 DEG C, reaction pressure 12MPa, volume space velocity 0.3h of reaction temperature in hydrogen decoloring reaction device 14~1, hydrogen
Oily ratio 900:1.
Reaction solution after hydrogenated decoloration is flashed into the second flash tank 15；Control the sudden strain of a muscle in second flash tank
Steam 180 DEG C of temperature, operating pressure 100kPa.Atent solvent is obtained at the top of the second flash tank, polymerization is pumped to by recycling
Solvent tank is recycled for polymerisation.
Hydrogenation resin liquid is obtained in the bottom of the second flash tank, send to vacuum distillation tower 16 and continues to remove oligomer；Control
180 DEG C of overhead temperature, operating pressure 10kPa；Oligomer is discharged in the tower top of destilling tower, the bottom of tower of destilling tower is melted
Melt resin obtains the light dicyclopentadiene petroleum resin of solid after cooling.It is 104 DEG C, Gardener to test its softening point
Coloration ＜ 1.
Embodiment 3
As shown in Figure 1, by dicyclopentadiene and No. 200 solvent naphthas by weight 45：After 55 mixing in input polymeric kettle 1,
Level stability is 60%, when being to slowly warm up to 250 DEG C with the speed of 2~3 DEG C/min, inlet valve and outlet valve is opened, by discharging
The residence time of Liquid level polymerisation raw material is 7h in valve opening and kettle.
In the unreacted gas phase reaction raw material of the top gas phase outlet discharge of polymeric kettle, enter condenser via pipeline,
Condensation enters back into dispenser to after 20~30 DEG C, and the liquid phase isolated and cyclopentadiene raw material enter after static mixer mixes,
Enter the polymeric kettle from the lower part of the polymeric kettle.
In the polymerization liquid uninterrupted pumping that polymeric kettle bottom obtains to the first flash tank 10, normal pressure removing accounts for raw material monomer
The unreacted monomer of 3.0wt%, after filtering out colloid and other impurities using 200 mesh filter screen filters, then with pipeline supplement account for
The atent solvent of polymerization liquid 5.0wt% enters together in the second static mixer 12 after mixing, extremely through the heat exchange of heat exchanger 13
130 DEG C, continuous conveying is extremely plus in hydrogen decoloring reaction device 14.Hydrogen is catalyzed by entering together with polymerization liquid after compressor boost
Agent bed, control add 230 DEG C, reaction pressure 10MPa, volume space velocity 0.7h of reaction temperature in hydrogen decoloring reaction device 14~1, hydrogen
Oily ratio 700:1.
Reaction solution after hydrogenated decoloration is flashed into the second flash tank 15；Control the sudden strain of a muscle in second flash tank
Steam 250 DEG C of temperature, operating pressure 100kPa.Atent solvent is obtained at the top of the second flash tank, polymerization is pumped to by recycling
Solvent tank is recycled for polymerisation.
Hydrogenation resin liquid is obtained in the bottom of the second flash tank, send to vacuum distillation tower 16 and continues to remove oligomer；Control
200 DEG C of overhead temperature, operating pressure 15kPa；Oligomer is discharged in the tower top of destilling tower, the bottom of tower of destilling tower is melted
Melt resin obtains the light dicyclopentadiene petroleum resin of solid after cooling.It is 110 DEG C, Gardener to test its softening point
Coloration ＜ 1.
Embodiment 4
As shown in Figure 1, by dicyclopentadiene and Isopar L atent solvents by weight 15：Polymeric kettle is put into after 85 mixing
In 1, level stability is 80%, when being to slowly warm up to 245 DEG C with the speed of 2~3 DEG C/min, opens inlet valve and outlet valve, by
The residence time of Liquid level polymerisation raw material is 20h in the valve opening that discharges and kettle.
In the unreacted gas phase reaction raw material of the top gas phase outlet discharge of polymeric kettle, enter condenser via pipeline,
Condensation enters back into dispenser to after 20~30 DEG C, and the liquid phase isolated and cyclopentadiene raw material enter after static mixer mixes,
Enter the polymeric kettle from the lower part of the polymeric kettle.
In the polymerization liquid uninterrupted pumping that polymeric kettle bottom obtains to the first flash tank 10, normal pressure removing accounts for raw material monomer
The unreacted monomer of 2.0wt%, after filtering out colloid and other impurities using 300 mesh filter screen filters, then with pipeline supplement account for
The atent solvent of polymerization liquid 2.0wt% enters together in the second static mixer 12 after mixing, extremely through the heat exchange of heat exchanger 13
170 DEG C, continuous conveying is extremely plus in hydrogen decoloring reaction device 14.Hydrogen is catalyzed by entering together with polymerization liquid after compressor boost
Agent bed, control add 240 DEG C, reaction pressure 6MPa, volume space velocity 0.5h of reaction temperature in hydrogen decoloring reaction device 14~1, hydrogen oil
Than 1000:1.
Reaction solution after hydrogenated decoloration is flashed into the second flash tank 15；Control the flash distillation temperature in the second flash tank
170 DEG C of degree, operating pressure 80kPa.Atent solvent is obtained at the top of the second flash tank, polymer solvent storage is pumped to by recycling
Tank is recycled for polymerisation.
Hydrogenation resin liquid is obtained in the bottom of the second flash tank, send to vacuum distillation tower 16 and continues to remove oligomer；Control
220 DEG C of overhead temperature, operating pressure 20kPa；Oligomer is discharged in the tower top of destilling tower, the bottom of tower of destilling tower is melted
Melt resin obtains the light dicyclopentadiene petroleum resin of solid after cooling.It is 107 DEG C, Gardener to test its softening point
Coloration ＜ 1.
Claims (5)
1. a kind of continuous method for preparing light dicyclopentadiene petroleum resin, it is characterised in that include the following steps：
Dicyclopentadiene feedstock and atent solvent are continuously introduced into reaction kettle and carry out thermal polymerization, it is slow with the speed of 2~3 DEG C/min
Be warming up to polymerization temperature, control polymerization temperature in the reaction kettle be 220~270 DEG C, it is 0.5~2.0MPa of reaction pressure, anti-
Answer 0.5~20.0h of residence time of liquid level material under 60~80%, polymerization temperature in kettle；Gathered in the outlet of reaction kettle
Close reaction solution；
The amount for controlling atent solvent described in reaction system in the polymeric kettle is 55~85wt% of reaction raw materials total amount；
The atent solvent in aromatic hydrocarbon, cycloalkane, linear paraffin, de- aromatic hydrocarbon aliphatic category and isomeric alkane hydro carbons extremely
Few one kind；
Obtained polymerization liquid is sent to the flash distillation removing of the first flash tank to the 0.5~4.0wt% unreacted lists for accounting for raw material monomer
After body, after filtering out colloid and other impurities using 100~400 mesh filter screen filters, into hydrogenation reactor；Control is described to add hydrogen
The reaction condition of reactor is：6.0~15.0MPa of reaction pressure, 200~280 DEG C of reaction temperature, 0.3~1.0h of volume space velocity~1, hydrogen-oil ratio 500:1~1000:1；Hydrogenation catalyst is loaded palladium catalyst, and the mass fraction of Pd is 0.5~2.0%, catalysis
Agent carrier is γ-Al2O3, and specific surface area is 80~250m2/g；
Add the hydrogenation resin liquid obtained after hydrogen to be delivered to the second flash tank and steam solvent, obtains flash distillation resin liquid；Control flash distillation temperature
170~200 DEG C of degree, 80~200kPa of flashing pressure；
The flash distillation resin liquid is delivered to destilling tower to be evaporated under reduced pressure, it is 180~220 to control the tower top temperature in destilling tower
DEG C, operating pressure is 10~20kPa, and oligomer is discharged from the tower top of destilling tower, and light color bicyclic penta is obtained in the bottom of tower of destilling tower
Diene Petropols.
2. according to the continuous method for preparing light dicyclopentadiene petroleum resin described in claim 1, it is characterised in that institute
It is petroleum cracking C5 mixtures to state dicyclopentadiene feedstock, in the dicyclopentadiene feedstock dicyclopentadiene content be 67~
87wt%.
3. according to the continuous method for preparing light dicyclopentadiene petroleum resin described in claim 1, it is characterised in that institute
State atent solvent be selected from benzene,toluene,xylene, trimethylbenzene, hexane, hexamethylene, heptane, octane, nonane, certain herbaceous plants with big flowers alkane, hendecane,
At least one in 12 carbon alkane, No. 100 solvent naphthas, No. 200 solvent naphthas, solvent D40, solvent D60, Isopar H and Isopar L
Kind.
4. according to the continuous method for preparing light dicyclopentadiene petroleum resin described in claim 1, it is characterised in that institute
The top gas phase outlet for stating polymeric kettle is sequentially connected condenser and dispenser, and the gaseous substance in the polymeric kettle is introduced through pipeline
Condenser is condensed to after 20~30 DEG C, and the liquid phase isolated and the cyclopentadiene raw material enter after static mixer mixes, from
The lower part of the polymeric kettle enters the polymeric kettle.
5. the continuous preparation method for preparing light dicyclopentadiene petroleum resin according to claim 1, it is characterised in that
The polymerization liquid for going out the polymeric kettle fills into atent solvent and enters repeated hydrogenation reactor after mixing；Fill into atent solvent
Amount be the polymerization liquid 0.5~5.0wt%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114716586A (en) * | 2022-04-22 | 2022-07-08 | 山东齐隆化工股份有限公司 | Process for the preparation of hydrogenated resins |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4604447A (en) * | 1983-11-22 | 1986-08-05 | Hercules Incorporated | Halogen-free, high flash point reactant solution |
| CN101555307A (en) * | 2009-05-09 | 2009-10-14 | 中国石油兰州石油化工公司 | Method for synthesizing poly-dicyclopentadiene petroleum resin with adjustable molecular weight, distribution and softening point |
| CN102558444A (en) * | 2010-12-17 | 2012-07-11 | 中国石油天然气股份有限公司 | Method for preparing dicyclopentadiene hydrogenated petroleum resin |
| CN203333552U (en) * | 2013-06-25 | 2013-12-11 | 朗盈科技（北京）有限公司 | Production system for synthesizing dicyclopentadiene petroleum resin |
| CN107252688A (en) * | 2017-05-15 | 2017-10-17 | 北京石油化工学院 | A kind of DCPD hydrogenation of petroleum resin catalyst and its preparation method and application |
-
2018
- 2018-03-07 CN CN201810186351.4A patent/CN108329429B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4604447A (en) * | 1983-11-22 | 1986-08-05 | Hercules Incorporated | Halogen-free, high flash point reactant solution |
| CN101555307A (en) * | 2009-05-09 | 2009-10-14 | 中国石油兰州石油化工公司 | Method for synthesizing poly-dicyclopentadiene petroleum resin with adjustable molecular weight, distribution and softening point |
| CN102558444A (en) * | 2010-12-17 | 2012-07-11 | 中国石油天然气股份有限公司 | Method for preparing dicyclopentadiene hydrogenated petroleum resin |
| CN203333552U (en) * | 2013-06-25 | 2013-12-11 | 朗盈科技（北京）有限公司 | Production system for synthesizing dicyclopentadiene petroleum resin |
| CN107252688A (en) * | 2017-05-15 | 2017-10-17 | 北京石油化工学院 | A kind of DCPD hydrogenation of petroleum resin catalyst and its preparation method and application |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114716586A (en) * | 2022-04-22 | 2022-07-08 | 山东齐隆化工股份有限公司 | Process for the preparation of hydrogenated resins |
| CN114716586B (en) * | 2022-04-22 | 2023-11-28 | 山东齐隆化工股份有限公司 | Process for producing hydrogenated resin |
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