CN104877077A - Method for preparing hydrogenated C9 petroleum resin - Google Patents
Method for preparing hydrogenated C9 petroleum resin Download PDFInfo
- Publication number
- CN104877077A CN104877077A CN201510354808.4A CN201510354808A CN104877077A CN 104877077 A CN104877077 A CN 104877077A CN 201510354808 A CN201510354808 A CN 201510354808A CN 104877077 A CN104877077 A CN 104877077A
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- resin
- catalyst
- content
- catalyzer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a method for preparing hydrogenated C9 petroleum resin, and belongs to the technical field of resin hydrogenation. A Ni/ZnO catalyst serves as a hydrogenation adsorption desulfurization catalyst, a supported metal catalyst serves as a hydrogenation decoloration catalyst, the resin is hydrogenated in a two-section fixed bed continuous hydrogenation mode, and due to the application of the Ni/ZnO hydrogenation adsorption desulfurization catalyst, the service life of the supported metal catalyst is guaranteed. The hue of the prepared hydrogenated resin is improved to be water white, and good heat stability is achieved. The method has the advantages that the process is simple, the activity of the catalysts is high, the chromaticity of the resin is improved, the heat stability of the resin is improved, the softening point is slightly reduced, and good economic benefits and industrial application prospects are achieved.
Description
Technical field
The invention belongs to Hydrogenation Technology of Petroleum Resin field, relate to a kind of method preparing hydrogenation C9 petroleum resin.
Background technology
Conventional resins is micro-Huang or brown due to outward appearance, greatly limit its application.And its degree of unsaturation reduces greatly after hydrogenation modification, resin becomes colourless, without special odor, the performance such as binding property, stability all increases, and has widened its Application Areas further.Compare in recent years it is emphasised that produce weather-proof resin, low viscosity resin, the copolymer resin of high softening-point, what stress in particular is the hydrogenated resin that look shallow.Hydrogenation modification is petroleum resin modified important method.The representative of external C5/C9 hydrogenation of petroleum resin modification at present has the companies such as american exxon, Yi Siman, Japanese waste river and Japanese bright dipping.In recent years along with the continuous competition with market of updating of production technology, petroleum resin more and more to mass-producing, seriation, become more meticulous and superior development, with fastest developing speed is light high-grade petroleum resin.China should give priority to high softening-point, low colourity weathering resistance resin from now on, and colourless hydrogenated petroleum resin and special petroleum resin are developing direction.Petroleum resin after current hydrogenation modification are more and more subject to market and welcome, and compared with can only selling for the situation of 7000-8000 yuan/ton with the low side resin of domestic production, the contour quality product of hydrogenated petroleum resin has sold for 18000 yuan/ton.Catalyzer is the key of hydrogenated petroleum resin technology, external use palladium series catalyst and nickel catalyst mostly, and the developing direction of hydrogenation catalyst is activity, stability, the minimizing side reaction of raising catalyzer and suitably reduces manufacturing cost from now on.China should accelerate the research of hydrogenation of petroleum resin catalyzer and the paces of hydrogenation catalyst production domesticization, promotes the popularization of hydrogenated petroleum resin technology and the reduction of product cost further.Fully utilize in symposial at Second Committee C5/C9 in 2011, participant expert also think, the high-quality such as colourless hydrogenated petroleum resin, special petroleum resin, high value added product are the development trends of petroleum resin from now on, and advise that domestic petroleum production of resins enterprise steps up to develop Hydrogenation Technology of Petroleum Resin.Because C9 resin contains tens to ppm sulphur up to a hundred and chlorine or fluorine etc., these poisonous substances have poisoning effect to noble metal catalyst, and catalyzer then can be made to produce for nickel catalyzator acid, therefore resin degradation is serious.
For abundant C9 resin recycling problem, we successfully develop using Ni/ZnO catalyzer as hydrogenation adsorption desulfurize catalyst, load type metal catalyst to decolour catalyzer as hydrogenation, two sections of fixed bed continuous hydrogenation modes are adopted to carry out hydrogenation reaction to resin, due to the use of Ni/ZnO hydrogenation adsorption desulfurize catalyst, ensure that the work-ing life of load type metal catalyst.Obtained hydrogenation resin, resin form and aspect are improved to water-white and have good thermostability.Following known technology, all comes with some shortcomings:
Chinese patent, publication number: CN1084521A introduces a kind of method of hydrotreating of high density raw material petroleum resin, and its operation is more, more loaded down with trivial details, and product quality is low.
Chinese patent, publication number: CN1084548A, introduce a kind of preparation method of hydrogenation of petroleum resin solvent, its operation is many, and waste liquid is many, and the softening temperature of the product obtained reduces serious.
Chinese patent, publication number: CN1699195A, introduce palladium ion type catalytic resin deoxidization by adding hydrogen processing method, its process will consume a large amount of water, and the resin quality obtained is low.
Chinese patent, publication number: CN1803871A, introduces the decolouring of a kind of C5 and C9 petroleum resin autoclave hydrogenation, except the method for look, although it has higher activity to adding hydrogen into resin, hydrogenation degraded is relatively more serious, and final resin yield is low, and softening temperature reduces serious.
Chinese patent, publication number: CN103386302A discloses a kind of hydrogenation of petroleum resin catalyzer, namely with Al
2o
3for carrier, carried noble metal Pd and oxides additive, the palladium metal crystallite that particle diameter is less than 3nm accounts for more than 90%, and its weak point is that catalyzer is for impurity S
2-tolerance difference and easy poisoning and deactivation, catalyst life receives impact.
Chinese patent, publication number: CN103386308A discloses a kind of C5 hydrogenation of petroleum resin nickel catalyzator, with activated carbon supported Ni, add the auxiliary agents such as Zn, Co and form non-crystaline amorphous metal nano particle, reaction conversion ratio and selectivity increase, but because it adopts small-sized tank reactor to carry out rhythmic reaction, do not carry out the concrete industrial applications performance test of catalyzer.
Summary of the invention
The invention provides the method for a kind of Hydrogenation for high-grade resin, solve the problems such as the low and deficiency in economic performance of product specification in resin transfer process.Wide scope of material of the present invention, is target product with high-grade resin, improves resin colourity, improve thermostability, and resin softening point reduces seldom, and product yield significantly improves.
Technical scheme of the present invention is as follows:
Resin in the present invention comprises C9 resin, C5C9 copolymer resins one wherein.
The method is using Ni/ZnO catalyzer as hydrogenation adsorption desulfurize catalyst, load type metal catalyst to decolour catalyzer as hydrogenation, adopts two sections of fixed bed hydrogenation modes to carry out hydrogenation reaction to resin, obtained hydrogenated resin, resin form and aspect are improved to water-white, and softening temperature slightly reduces.Its method steps is:
With solvent, petroleum resin are dissolved in dissolving tower, ratio shared by petroleum resin is 5%-30%, then the thionizer injecting and hydrogenation adsorption desulfurize catalyst is housed is mixed with hydrogen, hydrogenation adsorption desulfurize removes the sulphur in resin, feeding temperature 240-320 DEG C, hydrogen partial pressure 0.5-18MPa, volume space velocity 2-16h
-1, hydrogen to oil volume ratio 100-300:1; Hydrogenation adsorption desulfurize catalyst is Ni/ZnO catalyzer; After hydrogenation adsorption desulfurize, resin solution enters hydrogenation tower, carries out hydrogenation decolouring, feeding temperature 220-320 DEG C, hydrogen partial pressure 6-18MPa, volume space velocity 0.2-1.2h
-1, hydrogen to oil volume ratio 200-1000:1; The hydrogenation catalyzer used that decolours is load type metal catalyst; Resin solution after hydrogenation decolouring injects desolventizing tower, through air distillation, the product solvent that tower top distills out is played circulation and is again dissolved petroleum resin, bottom product enters volatilization tower, volatilization tower negative-pressure operation, volatilization tower tower top goes out the high boiling point organic compound that the resin cracking of hydrogenation decolorization PetroChina Company Limited. produces.Go out hydrogenation resin at the bottom of volatilization tower tower, resin form and aspect are improved to water white, and softening temperature slightly reduces.
Described solvent is one or more in hexanaphthene, methylcyclohexane, normal heptane, perhydronaphthalene.
Described hydrogenation adsorption desulfurize catalyst is Ni/ZnO catalyzer, and Ni loading is 15%-25%,
Carrier is the ZnO with central hole structure, and mesopore volume ratio accounts for more than 60% of total pore volume.
The described hydrogenation catalyzer used that decolours is load type metal catalyst, and load type metal catalyst is Pd, PtPd, Ni; Carrier is SiO
2, Al
2o
3or Al
2o
3-TiO
2.For Supported Pd-Catalyst, Pd content 0.5% ~ 4.5%; For loading type PtPd catalyzer, wherein Pt:Pd=1:4, Pt content 0.2% ~ 1.0%, Pd content 0.8% ~ 4.0%; For supported Ni catalyst, Ni content 35% ~ 45%.
The decolouring of described hydrogenation adsorption desulfurize, hydrogenation, desolventizing and devolatilization operate continuously.Owing to employing two-stage hydrogenation method in method provided by the invention, improve reactive behavior and selectivity and anti-impurity ability, the inventive method is for the wide adaptability of C9 petroleum resin raw material, adopt the C9 petroleum resin that thermopolymerization or catalyzed polymerization obtain, no matter foreign matter content height in resin solution, especially, when sulphur content is higher in resin solution, method provided by the invention all can be adopted to carry out two step hydrotreatments, obtain high performance C9 hydrogenated petroleum resin.By one-stage hydrogenation adsorption desulfurize, effectively protect noble metal catalyst and the nickel catalyzator of secondary hydrogenation, catalyst life is greatly improved.Thus the present invention has technique simply, and catalyst activity is high, good stability, improves resin colourity, improves resin thermostability, and its softening temperature slightly reduces, and has good economic benefit and prospects for commercial application.
Accompanying drawing explanation
Accompanying drawing is process flow diagram of the present invention.
In figure: 1 dissolves tower; 2 thionizers; 3 bleaching towers; 4 desolventizing towers; 5 volatilization towers.
Embodiment
Specific embodiments of the invention are described in detail below in conjunction with technical scheme and accompanying drawing.
Embodiment 1: with zinc nitrate and nickelous nitrate for precursor, adopt coprecipitation method to prepare the NiO/ZnO of different Ni loading, NiO/ZnO, at 350 DEG C of reductase 12 h, prepares Ni/ZnO catalyzer.See the following form 1 feedstock property and different Ni loading hydrogenation adsorption desulfurize effect, and reaction conditions is feeding temperature 260 DEG C, hydrogen partial pressure 1MPa, volume space velocity 6h
-1, hydrogen to oil volume ratio 200:1, resin concentration is 20%.See the following form resin properties after 1 resin raw material and hydrogenation adsorption desulfurize.
1. colour measurement is toluene solution and the standard Fe-Co color solution colorimetric that resin is made into 50wt%.
As shown in Table 1, take Ni/ZnO as hydrogenation adsorption desulfurize catalyst, sweetening effectiveness is obvious, has gone out most sulphur in resin.After desulfurization, resin form and aspect are substantially constant, and softening temperature slightly reduces, and bromine valency declines, and prove that Ni/ZnO has good hydrogenation effect, Ni loading is increased to 25% from 20%, and sweetening effectiveness does not increase substantially, and therefore we select the loading of Ni to be 20%.
Embodiment 2: with 20%Ni loading Ni/ZnO for hydrogenation adsorption desulfurize catalyst, investigates reaction conditions to the impact of sweetening effectiveness.See the following form resin properties after 2 desulfurization.
Embodiment 3: with 20%Ni loading Ni/ZnO for hydrogenation adsorption desulfurize catalyst, reaction conditions is feeding temperature 260 DEG C, hydrogen partial pressure 1MPa, volume space velocity 6h
-1, hydrogen to oil volume ratio 200:1, resin concentration is 20%.The product property that following table 3 obtains after seeing operation in 100 hours.
The experimental result of 100 hours as shown in Table 3, on Ni/ZnO reactive adsorption desulfurization catalyst in sulphur and bromine valency with start compared with test substantially constant, show that this technology has satisfactory stability.Run by the upper time, Catalyst Adsorption sulfur capacity reaches 20% of catalyst weight.
Embodiment 4: with loading type Pd, PtPd, Ni catalyzer for decolouring catalyzer; Carrier is Al
2o
3.At 18MPa and 240 DEG C, air speed 0.6h on the basis of embodiment 3
-1carry out hydrogenation decolorization experiment, for Supported Pd-Catalyst, Pd content 1%; For loading type PtPd catalyzer, wherein Pt:Pd=1:4, Pt content 0.2%, Pd content 0.8%; For supported Ni catalyst, Ni content 40%.The hydrogenated resin product property that following table 4 is shown in reaction process condition and finally obtains.
Thermostability: resin sample thermal treatment 5 hours at 175 DEG C, surveys its Fe-Co form and aspect.
As shown in Table 4, noble metal hydrogenation decolouring catalyzer, and metalNicatalyst all shows good hydrogenation decolorizing effect, product Heat stability is good.Loading type PtPd catalyzer shows best hydrogenation effect, and gained hydrogenated resin stability is the highest.
Embodiment 5: with loading type PtPd catalyzer for decolouring catalyzer; Relatively different carriers is on the impact of hydrogenation decolorizing effect.Reaction conditions is 18MPa and 240 DEG C, air speed 0.6h
-1, hydrogen-oil ratio 400.The hydrogenated resin product property that following table 4 is shown in reaction process condition and finally obtains.
As shown in Table 5, noble metal hydrogenation decolouring catalyzer, carrier is not obvious on the impact of hydrogenation decolorizing effect.Load Al
2o
3type PtPd catalyzer shows best hydrogenation effect, and gained hydrogenated resin stability is the highest.
Embodiment 6: with PtPd loaded catalyst for hydrogenation decolours catalyzer, Al
2o
3for carrier, investigate reaction conditions to the impact of sweetening effectiveness.See the following form the rear hydrogenated resin character of 6 hydrogenation decolouring.
Be reactive adsorption desulfurization catalyst as shown in Table 6 with Ni/ZnO, PtPd loaded catalyst is hydrogenation decolouring catalyzer, adopts two sections of fixed bed hydrogenation modes to carry out hydrogenation reaction to resin, obtained hydrogenated resin, resin form and aspect are improved to water-white, and softening temperature slightly reduces and has good thermostability.Reaction conditions has certain influence to obtained hydrogenated resin character.
Embodiment 7: with PtPd loaded catalyst for hydrogenation decolours catalyzer, Al
2o
3for carrier.On the basis of embodiment 3 and embodiment 5, reaction conditions is: feeding temperature 240 DEG C, hydrogen partial pressure 18MPa, volume space velocity 0.6h
-1, hydrogen to oil volume ratio 400:1, resin concentration is 20%.Following table 7 is shown in the rear hydrogenated resin character of 500 hydrogenation decolouring.
The experimental result of this process operation 500h as shown in Table 7, take Ni/ZnO as reactive adsorption desulfurization catalyst, PtPd loaded catalyst is hydrogenation decolouring catalyzer, two sections of fixed bed hydrogenation modes are adopted to carry out hydrogenation reaction to resin, obtained hydrogenated resin, resin form and aspect are improved to water-white, and softening temperature slightly reduces and has good thermostability.The above results shows that technology of the present invention has satisfactory stability, catalyzer long service life.
Claims (10)
1. prepare a method for hydrogenation C9 petroleum resin, it is characterized in that, step is as follows:
Dissolution with solvents petroleum resin are used in dissolving tower, ratio shared by petroleum resin is 5%-30%, then the thionizer injecting and hydrogenation adsorption desulfurize catalyst is housed is mixed with hydrogen, hydrogenation adsorption desulfurize removes the sulphur in resin, feeding temperature 240-320 DEG C, hydrogen partial pressure 0.5-18MPa, volume space velocity 2-16h
-1, hydrogen to oil volume ratio 100-300:1; Hydrogenation adsorption desulfurize catalyst is Ni/ZnO catalyzer; After hydrogenation adsorption desulfurize, resin solution enters hydrogenation tower, carries out hydrogenation decolouring, feeding temperature 220-320 DEG C, hydrogen partial pressure 6-18MPa, volume space velocity 0.2-1.2h
-1, hydrogen to oil volume ratio 200-1000:1; The hydrogenation catalyzer used that decolours is load type metal catalyst; Resin solution after hydrogenation decolouring injects desolventizing tower, through air distillation, the product solvent that tower top distills out is played circulation and is again dissolved petroleum resin, bottom product enters volatilization tower, volatilization tower negative-pressure operation, volatilization tower tower top goes out the high boiling point organic compound that the resin cracking of hydrogenation decolorization PetroChina Company Limited. produces; Go out hydrogenation resin at the bottom of volatilization tower tower, resin form and aspect are improved to water white, and softening temperature reduces.
2. method according to claim 1, is characterized in that, described petroleum resin comprise the one in C9 resin, C5C9 copolymer resins.
3. method according to claim 1 and 2, is characterized in that, described solvent is one or more mixing in hexanaphthene, methylcyclohexane, normal heptane, perhydronaphthalene.
4. method according to claim 1 and 2, is characterized in that, described Ni/ZnO catalyzer, and Ni loading is 15%-25%, and carrier is the ZnO with central hole structure, and mesopore volume ratio accounts for more than 60% of total pore volume.
5. method according to claim 3, is characterized in that, described Ni/ZnO catalyzer, and Ni loading is 15%-25%, and carrier is the ZnO with central hole structure, and mesopore volume ratio accounts for more than 60% of total pore volume.
6. the method according to claim 1 or 2 or 5, is characterized in that, described load type metal catalyst is Pd, PtPd, Ni; Carrier is SiO
2, Al
2o
3or Al
2o
3-TiO
2; Supported Pd-Catalyst, Pd content 0.5% ~ 4.5%; Loading type PtPd catalyzer, wherein Pt:Pd=1:4, Pt content 0.2% ~ 1.0%, Pd content 0.8% ~ 4.0%; Supported Ni catalyst, Ni content 35% ~ 45%.
7. method according to claim 3, is characterized in that, described load type metal catalyst is Pd, PtPd, Ni; Carrier is SiO
2, Al
2o
3or Al
2o
3-TiO
2; Supported Pd-Catalyst, Pd content 0.5% ~ 4.5%; Loading type PtPd catalyzer, wherein Pt:Pd=1:4, Pt content 0.2% ~ 1.0%, Pd content 0.8% ~ 4.0%; Supported Ni catalyst, Ni content 35% ~ 45%.
8. method according to claim 4, is characterized in that, described load type metal catalyst is Pd, PtPd, Ni; Carrier is SiO
2, Al
2o
3or Al
2o
3-TiO
2; Supported Pd-Catalyst, Pd content 0.5% ~ 4.5%; Loading type PtPd catalyzer, wherein Pt:Pd=1:4, Pt content 0.2% ~ 1.0%, Pd content 0.8% ~ 4.0%; Supported Ni catalyst, Ni content 35% ~ 45%.
9. the method according to claim 1,2,5,7 or 8, is further characterized in that: the decolouring of hydrogenation adsorption desulfurize, hydrogenation, desolventizing and devolatilization operate continuously.
10. method according to claim 6, is further characterized in that: the decolouring of hydrogenation adsorption desulfurize, hydrogenation, desolventizing and devolatilization operate continuously.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510354808.4A CN104877077B (en) | 2015-06-24 | 2015-06-24 | A kind of method for preparing hydrogenation C9 Petropols |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510354808.4A CN104877077B (en) | 2015-06-24 | 2015-06-24 | A kind of method for preparing hydrogenation C9 Petropols |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104877077A true CN104877077A (en) | 2015-09-02 |
| CN104877077B CN104877077B (en) | 2018-02-16 |
Family
ID=53944776
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510354808.4A Active CN104877077B (en) | 2015-06-24 | 2015-06-24 | A kind of method for preparing hydrogenation C9 Petropols |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104877077B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105175633A (en) * | 2015-09-08 | 2015-12-23 | 胡平 | Combined hydrotreatment method and hydrotreatment system for petroleum resin |
| CN105367714A (en) * | 2015-12-03 | 2016-03-02 | 大连理工大学 | Method for preparing hydrogenated DCPD resin |
| CN106832127A (en) * | 2017-02-10 | 2017-06-13 | 恒河材料科技股份有限公司 | A kind of method for orienting the standby hydrogenation C 9 petroleum resin of Hydrogenation |
| CN108102029A (en) * | 2016-11-24 | 2018-06-01 | 上海宝钢化工有限公司 | Production method of low-odor coumarone resin |
| CN110237843A (en) * | 2018-03-09 | 2019-09-17 | 中国石油化工股份有限公司 | A kind of nickel catalyst and its preparation method and application |
| CN111333752A (en) * | 2020-02-28 | 2020-06-26 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| CN111333751A (en) * | 2020-02-28 | 2020-06-26 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| CN111574645A (en) * | 2020-05-27 | 2020-08-25 | 大连理工大学 | Hydrogenation method for high-sulfur petroleum resin |
| GB2595369A (en) * | 2020-02-28 | 2021-11-24 | Univ Ningbo Technology | Method for hydrogenation catalysis of C9 resin |
| CN113880969A (en) * | 2021-11-08 | 2022-01-04 | 大连理工大学 | Method for preparing hydrogenated petroleum resin by hydrogenation of cold-polymerized petroleum resin |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030150778A1 (en) * | 1997-07-15 | 2003-08-14 | Haluska Jerry L. | Hydrogenation process for hydrocarbon resins |
| CN101475836A (en) * | 2009-01-19 | 2009-07-08 | 中国科学院山西煤炭化学研究所 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
| CN102746458A (en) * | 2011-11-08 | 2012-10-24 | 盘锦和运新材料有限公司 | Preparation method for hydrogenated C9 petroleum resin |
| CN102924659A (en) * | 2012-11-12 | 2013-02-13 | 中国石油化工股份有限公司 | Preparation method for C9 hydrogenation petroleum resin |
-
2015
- 2015-06-24 CN CN201510354808.4A patent/CN104877077B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030150778A1 (en) * | 1997-07-15 | 2003-08-14 | Haluska Jerry L. | Hydrogenation process for hydrocarbon resins |
| CN101475836A (en) * | 2009-01-19 | 2009-07-08 | 中国科学院山西煤炭化学研究所 | Hydrogenation adsorption desulphurization and catalytic hydro-dearomatization cascade reaction process |
| CN102746458A (en) * | 2011-11-08 | 2012-10-24 | 盘锦和运新材料有限公司 | Preparation method for hydrogenated C9 petroleum resin |
| CN102924659A (en) * | 2012-11-12 | 2013-02-13 | 中国石油化工股份有限公司 | Preparation method for C9 hydrogenation petroleum resin |
Non-Patent Citations (1)
| Title |
|---|
| 魏延雨: "Ni/ZnO反应吸附脱除汽油中硫化物的研究", 《中国优秀硕士学位论文全文数据库工程科技I辑》 * |
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105175633A (en) * | 2015-09-08 | 2015-12-23 | 胡平 | Combined hydrotreatment method and hydrotreatment system for petroleum resin |
| CN105367714A (en) * | 2015-12-03 | 2016-03-02 | 大连理工大学 | Method for preparing hydrogenated DCPD resin |
| CN105367714B (en) * | 2015-12-03 | 2018-04-27 | 大连理工大学 | A kind of method for preparing drogenated DCPD resin |
| CN108102029A (en) * | 2016-11-24 | 2018-06-01 | 上海宝钢化工有限公司 | Production method of low-odor coumarone resin |
| CN106832127A (en) * | 2017-02-10 | 2017-06-13 | 恒河材料科技股份有限公司 | A kind of method for orienting the standby hydrogenation C 9 petroleum resin of Hydrogenation |
| CN106832127B (en) * | 2017-02-10 | 2019-07-30 | 恒河材料科技股份有限公司 | A method of orientation plus hydrogen preparation hydrogenation C 9 petroleum resin |
| CN110237843A (en) * | 2018-03-09 | 2019-09-17 | 中国石油化工股份有限公司 | A kind of nickel catalyst and its preparation method and application |
| CN111333751A (en) * | 2020-02-28 | 2020-06-26 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| CN111333752A (en) * | 2020-02-28 | 2020-06-26 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| CN111333751B (en) * | 2020-02-28 | 2021-06-08 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| CN111333752B (en) * | 2020-02-28 | 2021-06-08 | 宁波工程学院 | Hydrogenation catalysis method of carbon nine resin |
| WO2021169015A1 (en) * | 2020-02-28 | 2021-09-02 | 宁波工程学院 | Method for hydrogenation catalysis of c9 resin |
| GB2595369A (en) * | 2020-02-28 | 2021-11-24 | Univ Ningbo Technology | Method for hydrogenation catalysis of C9 resin |
| US20220325010A1 (en) * | 2020-02-28 | 2022-10-13 | Ningbo University Of Technology | Catalytic hydrogenation method for carbon nine resin |
| GB2595369B (en) * | 2020-02-28 | 2022-11-23 | Univ Ningbo Technology | Catalytic hydrogenation method for carbon nine resin |
| US11958930B2 (en) | 2020-02-28 | 2024-04-16 | Ningbo University Of Technology | Catalytic hydrogenation method for carbon nine resin |
| CN111574645A (en) * | 2020-05-27 | 2020-08-25 | 大连理工大学 | Hydrogenation method for high-sulfur petroleum resin |
| CN111574645B (en) * | 2020-05-27 | 2021-04-20 | 大连理工大学 | Hydrogenation method for high-sulfur petroleum resin |
| CN113880969A (en) * | 2021-11-08 | 2022-01-04 | 大连理工大学 | Method for preparing hydrogenated petroleum resin by hydrogenation of cold-polymerized petroleum resin |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104877077B (en) | 2018-02-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104877077A (en) | Method for preparing hydrogenated C9 petroleum resin | |
| CN105367714A (en) | Method for preparing hydrogenated DCPD resin | |
| CN102391426B (en) | Method for performing hydrogenating pretreatment on C9 petroleum resin | |
| CN1772846A (en) | Coal tar hydrogenating modification catalyst and its prepn and application | |
| CN102311766B (en) | Class II active center hydrogenation catalyst start-up vulcanization method | |
| CN1962706A (en) | Process for preparing hydrogenated C5/C9 copolymerized petroleum resin | |
| CN104941649A (en) | Hydrogenation catalyst for petroleum resin and preparation method and application thereof | |
| CN100549139C (en) | A kind of two-segment hydrocracking method | |
| CN105296001A (en) | System for preparing aromatic hydrocarbons through hydrogenation catalytic reforming of coal tar and method | |
| CN105561993A (en) | Catalyst for producing ethyl alcohol and co-producing ethyl acetate through acetic acid hydrogenation and preparation method | |
| CN102039139A (en) | Hydrocarbon oil hydrogenation depickling catalyst and application thereof | |
| CN111234867B (en) | C for pyrolysis gasoline9+Method for hydrogenating distillate | |
| CN111574645B (en) | Hydrogenation method for high-sulfur petroleum resin | |
| CN107649169A (en) | A kind of catalyst of hydrogenation deoxidation reaction and its preparation method and application | |
| CN102633941B (en) | Method for preparing high-grade resin by catalytic hydrogenation | |
| CN102558444A (en) | Method for preparing dicyclopentadiene hydrogenated petroleum resin | |
| CN109261153B (en) | Supported nickel-based catalyst and preparation method and application thereof | |
| CN104744203A (en) | Method for preparing decahydronaphthalene by virtue of industrial naphthalene hydrogenation | |
| CN113042043A (en) | Ruthenium-based hydrogenation catalyst, aqueous solution of ruthenium-based hydrogenation catalyst, and preparation method and application of aqueous solution | |
| CN102211029B (en) | Preparation method of hydrodesulfurization sulfide catalyst for diesel oil | |
| CN1261543C (en) | Process for improving cetane number of diesel oil and reducing aromatic hydrocarbon of diesel oil simultaneously | |
| CN102921457A (en) | Preparation method of deodorizing activator for gasoline | |
| CN105413694A (en) | Catalyst for catalyzing hydrogenation of petroleum resin as well as preparation method and application thereof | |
| CN104119951A (en) | Device for preparing high-purity alkane solvent oil and preparation method of high-purity alkane solvent oil | |
| CN1234814C (en) | Hydrogenation of distilled oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 124221 Liaoning city of Panjin Province in the Liaodong Bay Area Road No. 2 Applicant after: Dalian University of Technology Address before: The Liaodong Bay area large 124221 Dalian Road, Liaoning city of Panjin province No. 2 Applicant before: Dalian University of Technology |
|
| COR | Change of bibliographic data | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |