CN1325525C - C5,C9 copolymerized petroleum resin preparation method - Google Patents
C5,C9 copolymerized petroleum resin preparation method Download PDFInfo
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- CN1325525C CN1325525C CNB2004100569112A CN200410056911A CN1325525C CN 1325525 C CN1325525 C CN 1325525C CN B2004100569112 A CNB2004100569112 A CN B2004100569112A CN 200410056911 A CN200410056911 A CN 200410056911A CN 1325525 C CN1325525 C CN 1325525C
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Abstract
The present invention relates to a preparation method for C9 modification C5 petroleum resin. The present invention uses C5 as main raw material and uses C9 as modification raw material; C9 active fractions are added into C5 active fractions to prepare the C9 modification C5 petroleum resin; AlCl3 is used as catalysts to copolymerize C5 petroleum resin and C9 petroleum resin with the characteristics of the C5 petroleum resin and the C9 petroleum resin; the C5 petroleum resin and the C9 petroleum resin are copolymerized so as to compensate for respective defects with advantages; the hue of the prepared resin is less than 10, the bromine number is less than 30, and the acid value is less than 1, the softening temperature is from 100 to 130 DEG C, the conversion rate of active constituents is as high as 80 to 90%, and the average molecular weight reaches more than 1000; the present invention can be widely used in paint, traffic paint and printing ink.
Description
Technical field
The present invention relates to a kind of preparation method of petroleum resin, particularly a kind of C
5, C
9The preparation method of copolymerized petroleum resin.
Background technology
Petroleum resin are originally for replacing rosin and derivative thereof to develop.But, develop very fast once appearance.In short decades, had suitable production level and output.Especially in the world industrial flourishing country, the petroleum resin products specification is many, and production equipment is on a grand scale.Have nine companies to produce petroleum resin as Japan, throughput reaches 1,000,000 tons/year.The Exxon of the U.S., He Gelisi, solid special; The CdF company of France; Also all there is the petroleum resin production equipment in main in the world petrochemical corporation (complex)s of a few family such as the ICI company of Britain.Ground such as China Taiwan and South Korea also produce C
9Petroleum resin.The unit and the producer of China's research and production petroleum resin are many, but industrial scale is little, and output is not high, and kind quantity is also well below external some flourishing company.The raw material of petroleum resin is by product C of cracker and system benzene device
5And C
9C
5And C
9Under Fred Er-Ke Laifuci (Friedel-Crafte) catalyst action, carry out its polyreaction and make petroleum resin.The U.S. is the country that researchs and develops petroleum resin the earliest, begins one's study in 1910, and the forties in 20th century, Picoo company was at first with its industrialization.After the sixties, the petroleum resin industry of states such as the U.S., West Europe, Japan has obtained development rapidly.To the end of the eighties, the overall throughput of state's petroleum resin such as U.S., day, English, method reaches 45.1 ten thousand t/a, and wherein the throughput of hydrogenated petroleum resin is 6.64 ten thousand t/a.In recent years, along with updating and the needs of market competition of technology, petroleum resin have developed into many kinds, many trades mark, broad-spectrum functional synthetic resins.China developed petroleum resin since 1964, had successively built up some small-sized production equipments, but since raw material sources and technical problem, slower development.Along with the raising year by year of developing rapidly of China's Petrochemical, particularly ethylene production capacity, cracking C
9The quantity of cut makes full use of this part resource and develops the attention that derived product more and more causes people in continuous increase.The domestic in recent years cracking C that utilizes
5And C
9Resource has successively successfully been developed decylization C
5Resin, mixed C
5Resin, pentadiene resin, dcpd resin and C
9The synthetic technology of aromatic hydrocarbons petroleum resin, the petroleum resin production equipment of the kiloton of having gone into operation and ten thousand tons.C at home
5, C
9Copolymerized petroleum resin does not form large scale of production, and the petroleum resin industry is still based on the aromatic hydrocarbons petroleum resin.In the existing patent of existing petroleum resin, to C
9The report of petroleum resin is more, and C
5, C
9Copolymerization seldom.In the purposes field of current petroleum resin, C wherein
5Petroleum resin, C
5, C
9Copolymerized petroleum resin, modification C
9Petroleum resin and hydrogenation oil C
9The use of resin is maximum, and China lacks C
5, C
9Copolymerized petroleum resin and hydrogenated petroleum resin product also depend on import in a large number.Therefore, exploitation and development C
5, C
9Copolymerized petroleum resin becomes a current important subject, changes the main unsettled situations of quality index such as the main petroleum resin products low softening point of China, color and luster be darker.
Summary of the invention
The object of the present invention is to provide a kind of preparation method simple, easy to operate, and have the C of high softening-point low color
5, C
9The preparation method of copolymerized petroleum resin.
For achieving the above object, the technical solution used in the present invention is: boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component; At first in having the reactor of stirring, be lower than add under 10 ℃ the condition mass percent be 8～10% toluene as solvent, add mass percent again and be 0.5～2% AlCl
3Catalyzer; Drip in toluene solvant after mass percent is 15～35% C9 with 2 droplets/second speed then, dripping mass percent with 1 droplet/second speed in toluene solvant again is 55～75% C5; Stir after dropwising, reacted 3～6 hours down, obtain polymer fluid at 40～60 ℃; Reacted polymer fluid poured in the separating funnel wash under 65～75 ℃-alkali cleaning-washing, this process hockets, and is washed neutrality until polymer fluid; To be washed till the neutral polymer fluid pours in the reactor, under 0.08～0.095Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam the cut temperature when rising to the highest 120～130 ℃ always, till no longer rising after descending again, after temperature drops to normal temperature, stop heating, pour out polymkeric substance, cooling back grind up does not get final product.
Another characteristics of the present invention are: alkali cleaning is that to add mass percent in polymer fluid be that 1～2.5% concentration is 5% Na0H solution.
1, raw materials pretreatment
The used experimental raw of the present invention is the by-product C that is provided by Lanzhou chemical industrial company
9And C
5Cut owing to be coarse raw materials, wherein has only a certain proportion of active ingredient, therefore, and at first to C
9And C
5Cut carries out feed purification respectively, and boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component, the refining C that obtains
5Alkene accounts for former C
550% of coarse raw materials, and C
9Account for 57%.
2, catalyzed polymerization
In having the reactor of agitator≤10 ℃ add down mass percents be 8～10% toluene as solvent, and then to add mass percent be 0.5～2% AlCl
3Catalyzer, first speed dropping mass percent with 2 droplets/second are 15～35% C
9, dripping mass percent with 1 droplet/second speed then is 55～75% C
5, dropwise the back and stir intensification, reacted 3～6 hours down at 40～60 ℃;
3. polymer fluid washing:
Reacted polymer fluid poured in the separating funnel under 65～75 ℃, wash-alkali cleaning-washing, alkali cleaning is that to add mass percent in polymer fluid be that 1～2.5% concentration is 5% NaOH solution, this process hockets, and is washed neutrality up to polymer fluid;
4. underpressure distillation:
Because behind catalyzed polymerization, leaving the inactive ingredients of not participating in polyreaction, raw material exists.This unreacted reactant such as insufficient removing not only can be reduced the softening temperature of resin, and performances such as the thermotolerance of resin and form and aspect are significantly reduced, and have therefore selected distillation under vacuum that it is removed.To be washed till the neutral polymer fluid and pour in the reactor, under 0.08～0.095Mpa, polymer fluid be added thermal distillation, steam always the cut temperature rise to the highest no longer rise after descending again till, after temperature drops to normal temperature, stop heating, pour out polymkeric substance, obtain product after the cooling.Entire synthesis process is divided into feed purification, catalyzed polymerization, polymer fluid washing and four steps of underpressure distillation, referring to Fig. 1.
Referring to Fig. 2, table 1 is the influence of catalyst levels to product yield.
Table 1 catalyst levels is to the influence of product yield
| Catalyst levels per-cent (%) | 0.5 | 1.0 | 1.5 | 2.0 | 2.5 | 3.0 |
| Productive rate (%) | 43 | 47 | 48 | 51 | 49 | 46 |
Among Fig. 2, temperature of reaction: 55 ℃, reaction times: 5h, C5/C9 volume ratio: 3: 1.As seen from Figure 2, product yield increases with the increase of catalyzer add-on, but when catalyst levels be about the raw material total amount 1～2% the time, it is not very greatly that product yield changes, and increases its consumption and has little significance.Catalyst quality per-cent was about 2% when product yield was the highest.
Referring to Fig. 3, table 2 is polymerization temperature influences to product yield and color
Table 2 is polymerization temperature influences to product yield and color
| Temperature (℃) | 40 | 50 | 55 | 60 | 65 | 70 |
| Productive rate (%) | 35.2 | 40 | 48.5 | 51.1 | 47.5 | 43.3 |
| Color | Brown | Brown | Pale brown look | Faint yellow | Pale brown look | Pale brown look |
Among Fig. 3, AlCl
3Percentage composition be: 2%, reaction times: 5h, C5/C9 volume ratio: 3: 1.Along with the rising of temperature, polymer yield raises as seen from Figure 3, and color also shoals.But the too high easy generation implode of temperature, and C
5Cut can a large amount of evaporations, also can find out 60 ℃ from the figure after productive rate descend to some extent on the contrary, so temperature is 60 ℃ and is advisable.In addition, drip the raw material process and want the controlled temperature can not be too high, otherwise the implode phenomenon takes place easily.
Referring to Fig. 4, table 3 is the influences to productive rate of time reflection time
Keeping temperature of reaction is 60 ℃, changes the differential responses time, productive rate such as table 3 and shown in Figure 4:
Table 3 reaction times is to the influence of productive rate
| Reaction times (h) | 3 | 3.5 | 4 | 4.5 | 5 | 6 |
| Productive rate (%) | 42.3 | 46.5 | 51.4 | 51.8 | 52 | 52.2 |
Among Fig. 4, AlCl
3Percentage composition be: 2%, temperature of reaction: 60 ℃, C5/C9 volume ratio: 2.5: 1.Reaction times is that 4 hours productive rates are higher as seen from Figure 4, after 4 hours the increase of productive rate very little, the time dropwises with raw material and begins to calculate after being warmed up to constant temperature.
Referring to Fig. 5, table 4 is C
5And C
9Volume ratio to the influence of productive rate
When 60 ℃ of temperature maintenance constant, C
5And C
9Volume ratio the influence of productive rate is seen Table 4 and Fig. 5.
Table 4 C
5And C
9Volume ratio to the influence of productive rate
| C 5/C 9Volume ratio | 1.5∶1 | 2∶1 | 2.5∶1 | 3∶1 | 3.6∶1 | 4∶1 |
| Productive rate (%) | 46.2 | 47.5 | 51.5 | 49 | 46.8 | 46.2 |
Among Fig. 5, AlCl
3Percentage composition be: 2%, temperature of reaction: 60 ℃, the reaction times: 4h.As seen from Figure 5, when the volume of C5/C9 increased, productive rate raise, and is that 2.5: 1 o'clock productive rates reach maximum value in the C5/C9 volume ratio, reduced C with the increase of C5/C9 volume ratio again afterwards
5And C
9Volume ratio can be controlled in 2: 1～3: 1.
By above each influence factor as can be known, work as C
5And C
9Volume ratio be controlled at 2: 1～3: 1, temperature of reaction is 60 ℃, catalyst levels is about 1～2% of raw material total amount, the reaction times was controlled at about 4 hours, productive rate reaches as high as 51%;
This invented technology is simple, and is easy to operate, and polymer fluid washs not emulsification, and layering is very fast; With AlCl
3Be prepared resin form and aspect＜10 of catalyzer, bromine number＜30, acid number＜1, softening temperature is between 100-130 ℃, and the active ingredient transformation efficiency is up to 80-90%, and molecular-weight average reaches more than 1000, can be widely used in paint, traffic paint and the printing-ink.
The present invention is with C
5Be main raw material, with C
9Be modified feedstock, at C
5Add C in the active fractions
9Active fractions, preparation C
9Modification C
5Petroleum resin are with AlCl
3Be catalyzer copolymerization C
5, C
9Petroleum resin have C concurrently
5Petroleum resin and C
9The characteristic of petroleum resin, can utilize separately advantage to remedy separately deficiency both copolymerization, prepared resin form and aspect＜10, bromine number＜30, acid number＜1, softening temperature are between 100-130 ℃, and the active ingredient transformation efficiency is up to 80-90%, molecular-weight average reaches more than 1000, can be widely used in paint, traffic paint and the printing-ink.
Description of drawings
Fig. 1 is C of the present invention
9Modification C
5The polymerization schema of petroleum resin;
Fig. 2 is the influence figure of catalyst levels of the present invention to product yield;
Fig. 3 is the influence figure of polymerization temperature of the present invention to product yield;
Fig. 4 is the influence figure of polymerization time of the present invention to product yield;
Fig. 5 is C of the present invention
5And C
9Volume ratio to the figure that influences of product yield.
Embodiment
Embodiment 1
Boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component; At first in having the reactor of stirring (the agitator model is 60W, 3000 rev/mins, Changzhou state China motor company), be lower than add under 10 ℃ the condition mass percent be 10% toluene as solvent, add mass percent again and be 2% AlCl
3Catalyzer; Drip in toluene solvant after mass percent is 30% C9 with 2 droplets/second speed then, dripping mass percent with 1 droplet/second speed in toluene solvant again is 60% C5; Stir after dropwising, reacted 6 hours down, obtain polymer fluid at 60 ℃; Reacted polymer fluid poured in the separating funnel wash under 75 ℃-alkali cleaning-washing, alkali cleaning is that to add mass percent in polymer fluid be 5% NaOH solution, and this process hockets, and is washed neutrality until polymer fluid; To be washed till the neutral polymer fluid pours in the reactor, under 0.095Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam the cut temperature when rising to the highest 120 ℃ always, till no longer rising after the decline, after temperature drops to normal temperature, stop heating, pour out polymkeric substance, being crushed into powder after the cooling gets final product.
Embodiment 2
Boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component; At first in having the reactor of stirring, be lower than add under 10 ℃ the condition mass percent be 8% toluene as solvent, add mass percent again and be 1% AlCl
3Catalyzer; Drip in toluene solvant after mass percent is 33% C9 with 2 droplets/second speed then, dripping mass percent with 1 droplet/second speed in toluene solvant again is 66% C5; Stir after dropwising, reacted 5 hours down, obtain polymer fluid at 50 ℃; Reacted polymer fluid poured in the separating funnel wash under 65～75 ℃-alkali cleaning-washing, this process hockets, and is washed neutrality until polymer fluid; To be washed till the neutral polymer fluid pours in the reactor, under 0.08Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam the cut temperature when rising to the highest 120 ℃ always, till no longer rising after the decline, after the cut temperature drops to normal temperature, stop heating, pour out polymkeric substance, being crushed into powder after the cooling gets final product.
Embodiment 3
Boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component; At first in having the reactor of stirring, be lower than add under 10 ℃ the condition mass percent be 9% toluene as solvent, add mass percent again and be 0.5% AlCl
3Catalyzer; Drip in toluene solvant after mass percent is 16% C9 with 2 droplets/second speed then, dripping mass percent with 1 droplet/second speed in toluene solvant again is 74.5% C5; Stir after dropwising, reacted 3 hours down, obtain polymer fluid at 40 ℃; Reacted polymer fluid poured in the separating funnel wash under 65 ℃-alkali cleaning-washing, this process hockets, and is washed neutrality until polymer fluid; To be washed till the neutral polymer fluid pours in the reactor, under 0.09Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam the cut temperature when rising to the highest 120 ℃ always, till no longer rising after the decline, after the cut temperature drops to normal temperature, stop heating, pour out polymkeric substance, being crushed into powder after the cooling gets final product.
Embodiment 4
Boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component; At first in having the reactor of stirring, be lower than add under 10 ℃ the condition mass percent be 10% toluene as solvent, add mass percent again and be 2% AlCl
3Catalyzer; Drip in toluene solvant after mass percent is 25.5% C9 with 2 droplets/second speed then, dripping mass percent with 1 droplet/second speed in toluene solvant again is 62.5% C5; Stir after dropwising, reacted 4 hours down, obtain polymer fluid at 60 ℃; Reacted polymer fluid poured in the separating funnel wash under 70 ℃-alkali cleaning-washing, this process hockets, and is washed neutrality until polymer fluid; To be washed till the neutral polymer fluid pours in the reactor, under 0.095Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam always the cut temperature rise to the highest no longer rise after descending again till, after the cut temperature drops to normal temperature, stop heating, pour out polymkeric substance, being crushed into powder after the cooling gets final product.
Claims (2)
1, a kind of C
5, C
9The preparation method of copolymerized petroleum resin is characterized in that:
1) raw materials pretreatment
Boiling point is 40-70 ℃ C under the collection normal pressure
5Boiling point was 90-120 ℃ C when alkene and vacuum tightness were 0.09MPa
9Olefin component;
2) catalyzed polymerization
At first in having the reactor of stirring, be lower than add under 10 ℃ the condition mass percent be 8～10% toluene as solvent, add mass percent again and be 0.5～2% AlCl
3Catalyzer;
Dripping mass percent with 2 droplets/second speed in toluene solvant then is 15～35% C
9Behind the alkene, dripping mass percent with 1 droplet/second speed in toluene solvant again is 55～75% C
5Alkene;
Stir after dropwising, reacted 3～6 hours down, obtain polymer fluid at 40～60 ℃;
3) polymer fluid washing
Reacted polymer fluid poured in the separating funnel wash under 65～75 ℃-alkali cleaning-washing, this process hockets, and is washed neutrality until polymer fluid;
4) underpressure distillation
To be washed till the neutral polymer fluid pours in the reactor, under 0.08～0.095Mpa, polymer fluid is added thermal distillation, Heating temperature is less than 50 ℃, steam the cut temperature rises to the highest always, and till the decline of cut temperature is no longer risen, after the cut temperature drops to normal temperature, stop heating, pour out polymkeric substance, being crushed into powder after the cooling gets final product.
2, C according to claim 1
5, C
9The preparation method of copolymerized petroleum resin is characterized in that: said alkali cleaning is that to add mass percent in polymer fluid be that 1～2.5% concentration is 5% NaOH solution.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100569112A CN1325525C (en) | 2004-08-20 | 2004-08-20 | C5,C9 copolymerized petroleum resin preparation method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100569112A CN1325525C (en) | 2004-08-20 | 2004-08-20 | C5,C9 copolymerized petroleum resin preparation method |
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|---|---|
| CN1737026A CN1737026A (en) | 2006-02-22 |
| CN1325525C true CN1325525C (en) | 2007-07-11 |
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|---|---|---|---|
| CNB2004100569112A Expired - Fee Related CN1325525C (en) | 2004-08-20 | 2004-08-20 | C5,C9 copolymerized petroleum resin preparation method |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101700990B (en) * | 2009-11-03 | 2012-09-26 | 浙江恒河石油化工股份有限公司 | Method for preparing C9 petroleum resin with light color and high softening-point |
| CN102643389B (en) * | 2011-02-22 | 2013-11-06 | 中国石油天然气股份有限公司 | Preparation method for petroleum resin with high softening point |
| CN106699972B (en) * | 2016-11-17 | 2019-04-12 | 恒河材料科技股份有限公司 | A kind of preparation method and its device of C5/C10 copolymer resins |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6264811A (en) * | 1985-09-17 | 1987-03-23 | Toho Chem Ind Co Ltd | Production of light-color petroleum resin for paint |
| CN1288017A (en) * | 2000-10-13 | 2001-03-21 | 山西省应用化学研究所 | Alkyl phenolic modified petroleum resin and its prepn. method |
| CN1356346A (en) * | 2001-12-14 | 2002-07-03 | 耿朝华 | Process for synthesizing petroleum resin by thermal polymerization method |
-
2004
- 2004-08-20 CN CNB2004100569112A patent/CN1325525C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6264811A (en) * | 1985-09-17 | 1987-03-23 | Toho Chem Ind Co Ltd | Production of light-color petroleum resin for paint |
| CN1288017A (en) * | 2000-10-13 | 2001-03-21 | 山西省应用化学研究所 | Alkyl phenolic modified petroleum resin and its prepn. method |
| CN1356346A (en) * | 2001-12-14 | 2002-07-03 | 耿朝华 | Process for synthesizing petroleum resin by thermal polymerization method |
Non-Patent Citations (4)
| Title |
|---|
| C5/C9共聚石油树脂的合成研究 刘进锋，贵州化工，第27卷第5期 2002 * |
| C5/C9共聚石油树脂的合成研究 刘进锋，贵州化工，第27卷第5期 2002;合成C5-C9混合石油树脂 孙立欣 武兴彬 于涛 刘海同 姜公和，化学与粘合，第4期 2000;袭解C5 C9镏分共聚石油树脂的研究 侯长利 邢进 赵春立，齐齐哈尔大学学报，第16卷第1期 2000 * |
| 合成C5-C9混合石油树脂 孙立欣 武兴彬 于涛 刘海同 姜公和，化学与粘合，第4期 2000 * |
| 袭解C5 C9镏分共聚石油树脂的研究 侯长利 邢进 赵春立，齐齐哈尔大学学报，第16卷第1期 2000 * |
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