CN102504107A - Continuous production method and continuous water washing method for C5 petroleum resin - Google Patents
Continuous production method and continuous water washing method for C5 petroleum resin Download PDFInfo
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Abstract
The invention aims to increase production efficiency of C5 petroleum resin and reduce water consumption for water washing, and provides continuous water washing method and continuous polymerization method in C5 petroleum resin production. The continuous production method comprises the following steps of: pre-preparing catalysts, and performing continuous polymerization and heat-insulation polymerization of decyclized C5 fraction; then washing with alkaline water, clear water and ammonia water in sequence; and finally drying and molding to obtain C5 petroleum resin. The methods provided by the invention can achieve full automatic control of the whole operation process, have high daily yield and low labor intensity, make product quality more stable and better, reduce consumptions of catalysts and alkaline water by 30% to 40% as compared with the intermittent method, reduce power consumption by 30%, and protect equipment against corrosion.
Description
Technical field
The present invention relates to a kind of C 5 petroleum resin working method, more particularly, the present invention relates to a kind of C 5 petroleum resin continuous production method and continuous washing method.
Background technology
Now, C 5 petroleum resin all adopts the batchwise polymerization method to produce in the industry.With the aluminum trichloride (anhydrous) is catalyzer, carries out cationic polymerization, and the washing that neutralizes after the polymerization is to remove catalyzer.Polymerization process with in water washing process all adopt the periodical operation process.Polymerization process is in the carbon steel polymeric kettle that band stirs, to carry out.In be in the stainless steel still that three bands stir, to divide three steps to carry out with water washing process.
At first, the solvent in the solvent test tank is added in the polymeric kettle quantitatively.Start stirring, under agitation add Catalyzed by Anhydrous Aluminium Chloride agent (aluminum chloride by each still quantitative package good then once add), temperature in the kettle should be controlled at 20～50 ℃ at this moment.Then carbon Wuyuan material is added in the polymeric kettle through carbon five fresh feed pumps continuously and quantitatively.Along with the adding of carbon five material, polyreaction begins, and temperature constantly raises, and temperature of reaction is controlled at 80～90 ℃.The carbon slender acanthopanax material time was controlled at about 4 hours, and material adds back insulation 30 minutes, 80～85 ℃ of temperature.Polyreaction is delivered to polymerization liquid in the neutralizing well after finishing, and the washing of preparing to neutralize is to remove catalyzer.
In be divided into three times and carry out with water washing process, be followed successively by: alkali cleaning-washing-washing.Particularly, during the alkali lye of concentration 5% squeezed into quantitatively and still, and add the emulsion splitter for preparing.Start stirring, the chuck with still in inciting somebody to action simultaneously feeds steam, and temperature in the kettle remains on 60～80 ℃, stirs to stop after 20 minutes stirring.Material left standstill 30 minutes under 70～75 ℃ of conditions in the still.Then following water layer is carried out layering through visor manual observation, drain into waste water processing station after the layering.During remaining oil reservoir is still stayed and still, prepare to proceed twice washing.In the soft water of water softening tank being squeezed into quantitatively and still, add the emulsion splitter for preparing, other operation steps is identical with alkali cleaning again.After each washing was left standstill, the water stratification below visor manual observation drained into waste water processing station after the layering.Polymerization liquid is pressed into the resin settled flow container through self pressure.
In sum, available technology adopting batchwise polymerization and method for washing production at intermittence C 5 petroleum resin exist problems; Production efficiency is low, and labour intensity is big, belongs to the labour-intensive mode of production; The reference mark of polymerization and washing is repeated low at every turn; Cause unstable product quality easily, product yield is low, thereby influences productivity effect and output.And intermittently the water consumption of method for washing is bigger, and the wastewater treatment expense has become an outstanding problem.In recent years, the demand of China's C 5 petroleum resin significantly increases, and supply falls short of demand, and substantial appreciation of prices, and causing production efficiency is exactly the situation of benefit and profit.In order to improve turnout and further to increase profit margin, need the continuous production method and the continuous washing method of a kind of high efficiency C 5 petroleum resin of exploitation.
Summary of the invention
For production efficiency that improves C 5 petroleum resin and the water consumption that reduces washing, the contriver has developed continuous washing method and continuous polymerization method in a kind of C 5 petroleum resin production through TE and further investigation.
Concrete technical scheme is following:
Continuous washing method in the C 5 petroleum resin production process of the present invention may further comprise the steps:
(1) alkali cleaning: be that the buck of 40～55 ℃ mass percent concentration 2% gets in first mixed flow device and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 4～6: 1, gets into buck sedimentation tower middle part then, polymerization liquid and buck in buck sedimentation tower through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(2) washing: second the mixed flow device of water entering that is 40～55 ℃ by polymer resin liquid I and the temperature of buck sedimentation column overhead extraction; The volume ratio 4～6: 1 of polymer resin liquid I and water; In second mixed flow device, mix, get into clear water sedimentation tower then, through layering; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II;
(3) ammonia scrubbing: the ammoniacal liquor resin liquid of the mass percent concentration 0.3%～0.5% that is 40～55 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation column overhead extraction gets into the 3rd mixed flow device; The volume ratio 4～6: 1 of polymer resin liquid II and water; In the 3rd mixed flow device, mix, get into ammoniacal liquor sedimentation tower then, by discharging waste water at the bottom of the tower; By cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
The temperature of preferably, said (1) alkali cleaning, (2) washing and (3) ammonia scrubbing step is 47～53 ℃.
Preferably, said buck is the aqueous solution of sodium hydroxide.
Preferably, the height of said buck sedimentation tower, clear water sedimentation tower and ammoniacal liquor sedimentation tower is respectively 5～20 meters.The residence time of polymerization liquid in each sedimentation tower was generally 0.3～3 hour, preferred 0.5～2 hour.
Continuous washing method of the present invention can be used for the process that prior art discontinuous method is produced C 5 petroleum resin.
In order to improve the production efficiency of C 5 petroleum resin; The contriver is applied in above-mentioned continuous washing method in the C 5 petroleum resin process; And the continuous polymerization method of decylization C5 fraction proposed; The two is integrated, formed the continuous production method of C 5 petroleum resin, concrete technical scheme is following:
The continuous production method of C 5 petroleum resin of the present invention may further comprise the steps:
(1) catalyzer preformulation: with nitrogen the catalyzer aluminum trichloride (anhydrous) is pressed in the catalyzer still, mixes through the refrigerative polymerization liquid with coming the self-heat conserving polymeric kettle, the quality of said aluminum trichloride (anhydrous) is 1% of a polymerization liquid quality;
(2) polyreaction: the mixed solution in the catalyzer still is delivered to polymerization reaction kettle with catalyst pump; Simultaneously the decylization cracked C 5 fraction is added in the polymerization reaction kettle; Temperature of reaction is controlled at 65～75 ℃; The adding weight of catalyzer aluminum trichloride (anhydrous) is 0.3%～0.35% of decylization cracked C 5 fraction add-on, and unpolymerized C 5 diene content is 13wt%～17wt% to the adding speed of control decylization cracked C 5 fraction in the polymerization reaction kettle to keep;
(3) insulation polymerization: the polymer fluid in the polymerization reaction kettle is delivered to the insulation polymeric kettle through water cooler with the reaction kettle recycle pump; The temperature of insulation polymeric kettle is controlled at 65～75 ℃; The transfer rate of controlled polymerization liquid makes the unpolymerized C 5 diene content≤2wt% in the insulation polymeric kettle; Deliver to the catalyzer still with the preparation catalyzer with insulation polymeric kettle recycle pump with partially polymerized liquid and after cooling off, all the other deliver to the washing unit;
(4) alkali cleaning: be that the buck of 40～55 ℃ mass percent concentration 2% gets in first mixed flow device and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 4～6: 1, gets into buck sedimentation tower middle part then, polymerization liquid and buck in buck sedimentation tower through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(5) washing: second the mixed flow device of water entering that is 40～55 ℃ by polymer resin liquid I and the temperature of buck sedimentation column overhead extraction; The volume ratio 4～6: 1 of polymer resin liquid I and water; In second mixed flow device, mix, get into clear water sedimentation tower then, through layering; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II;
(6) ammonia scrubbing: the ammoniacal liquor resin liquid of the mass percent concentration 0.3%～0.5% that is 40～55 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation column overhead extraction gets into the 3rd mixed flow device; The volume ratio 4～6: 1 of polymer resin liquid II and water; In the 3rd mixed flow device, mix, get into ammoniacal liquor sedimentation tower then, by discharging waste water at the bottom of the tower; By cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
Preferably, said polymer resin liquid III sedimentation after drying, moulding in the sedimentation storage tank make C 5 petroleum resin.
Said decylization C5 fraction is meant the cut after the C5 fraction of oil boom cracking generation removes cyclopentadiene and NSC 7352; Mainly contain C 5 alkane, carbon pentaene hydrocarbon and components such as m-pentadiene and isoprene; Those skilled in the art also know; Further do not contain the isoprene component in this cut and be fine yet, therefore in the scope of indication of the present invention yet.
Continuous production method of the present invention and continuous washing method have the following advantages:
1. successive reaction and continuous washing method can realize a complete set of operation sequence fully automated control, and quality product is more stable, and product quality is better.
2. add catalyzer and do not need to open again the manhole of reaction kettle, the potential safety hazard of having avoided unnecessary material loss and oil gas volatilization to bring.
3. the consumption of catalyzer and buck is 60～70% of a discontinuous method, and power consumption reduces by 30%, meets the policy requirements of national energy-saving and emission-reduction.
4. under the identical place and fund input, the output of continuous production method is the twice of discontinuous method.A complete set of operation sequence fully automated control realizes having reduced operator and is equipped with and labour intensity.
5. the washing of the 3rd step is used lower concentration ammoniacal liquor instead and can be removed residue trace chloride and cl ions in the polymer fluid, has solved the difficult problem of equipment corrosion all the time.
Description of drawings
Fig. 1 is the schematic flow sheet of C 5 petroleum resin continuous production method of the present invention.
Fig. 2 is the schematic flow sheet of continuous washing method in the C 5 petroleum resin production process of the present invention.
Nomenclature among the figure:
1: the catalyzer storage tank; 2: the catalyzer still; 3: catalyst pump; 4: polymerization reaction kettle; 5: the polymerization reaction kettle recycle pump; 6,9: water cooler; 7: the insulation polymeric kettle; 8: polymerization insulation still recycle pump; 10: first mixed flow device; 11: buck sedimentation tower; 12: the second mixed flow devices; 13: clear water mixed flow device; 14: the three mixed flow devices; 15: ammoniacal liquor sedimentation tower.
Embodiment
Further explain and explain C 5 petroleum resin continuous production method of the present invention and continuous washing method below in conjunction with accompanying drawing and embodiment.
Shown in the schematic flow sheet of Fig. 1 and 2, method of the present invention may further comprise the steps, but is not limited to shown in Fig. 1 and 2:
(1) catalyzer preformulation: the catalyzer aluminum trichloride (anhydrous) that will be stored in the catalyzer storage tank 1 with nitrogen is pressed in the catalyzer still 2; Mix through the refrigerative polymerization liquid with coming self-heat conserving polymeric kettle 7, the quality of said aluminum trichloride (anhydrous) is 1% of a polymerization liquid quality;
(2) polyreaction: the mixed solution in the catalyzer still 2 is delivered to polymerization reaction kettle 4 with catalyst pump 3; Simultaneously the decylization cracked C 5 fraction is added in the polymerization reaction kettle 4; Temperature of reaction is controlled at 65～75 ℃; The adding weight of catalyzer aluminum trichloride (anhydrous) is 0.3%～0.35% of decylization cracked C 5 fraction add-on, and unpolymerized C 5 diene content is 13wt%～17wt% to the adding speed of control decylization cracked C 5 fraction in the polymerization reaction kettle to keep; Temperature of reaction can adopt polymerization reaction kettle recycle pump 5 to make reaction solution water cooler 6 cooling of flowing through, and returns the mode of polymerization reaction kettle 4 then and controls;
(3) insulation polymerization: the polymer fluid in the polymerization reaction kettle 4 is delivered to insulation polymeric kettle 7 through water cooler 6 with polymerization reaction kettle recycle pump 5; The temperature of insulation polymeric kettle 7 is controlled at 65～75 ℃; The transfer rate of controlled polymerization liquid makes unpolymerized C 5 diene content≤2% in the insulation polymeric kettle; Make the polymer fluid water cooler 9 of flowing through with insulation polymeric kettle recycle pump 8, after the cooling, a part is delivered to catalyzer still 2 with the preparation catalyzer; A part is returned insulation polymeric kettle 7 with control reaction temperature, and all the other deliver to the washing unit;
(4) alkali cleaning: be that the buck of 40～55 ℃ mass percent concentration 2% gets in first mixed flow device 10 and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 4～6: 1, gets into buck sedimentation tower 11 middle parts then, polymerization liquid and buck in buck sedimentation tower 11 through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(5) washing: second the mixed flow device 12 of water entering that is 40～55 ℃ by polymer resin liquid I and the temperature of buck sedimentation tower 11 cat head extraction; The volume ratio 4～6: 1 of polymer resin liquid I and water; In second mixed flow device 12, mix, get into clear water sedimentation tower 13 then, through layering; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II;
(6) ammonia scrubbing: the ammoniacal liquor resin liquid of the mass percent concentration 0.3%～0.5% that is 40～55 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation tower 13 cat head extraction gets into the 3rd mixed flow device 14; The volume ratio 4～6: 1 of polymer resin liquid II and water; In the 3rd mixed flow device 14, mix, get into ammoniacal liquor sedimentation tower 15 then, by discharging waste water at the bottom of the tower; By cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
Said polymer resin liquid III sedimentation after drying, moulding in the sedimentation storage tank make C 5 petroleum resin.
(1) catalyzer preformulation: the catalyzer aluminum trichloride (anhydrous) that will be stored in the catalyzer storage tank 1 with nitrogen is pressed in the catalyzer still 2 with the speed of 1kg/h; Mix through the refrigerative polymerization liquid with coming self-heat conserving polymeric kettle 7, the quality of said aluminum trichloride (anhydrous) is 1% of a polymerization liquid quality;
(2) polyreaction: the mixed solution in the catalyzer still 2 is delivered to polymerization reaction kettle 4 with catalyst pump 3; Simultaneously the decylization cracked C 5 fraction is added in the polymerization reaction kettle 4; Temperature of reaction is controlled at 70 ℃; The adding weight of catalyzer aluminum trichloride (anhydrous) is 0.32% of decylization cracked C 5 fraction add-on, and unpolymerized C 5 diene content is about 15wt% to the adding speed of control decylization cracked C 5 fraction in the polymerization reaction kettle to keep; Temperature of reaction adopts polymerization reaction kettle recycle pump 5 to make reaction solution water cooler 6 coolings of flowing through, and returns the mode of polymerization reaction kettle 4 then and controls;
(3) insulation polymerization: the polymer fluid in the polymerization reaction kettle 4 is delivered to insulation polymeric kettle 7 through water cooler 6 with polymerization reaction kettle recycle pump 5; The temperature of insulation polymeric kettle 7 is controlled at 70 ℃; The transfer rate of controlled polymerization liquid makes unpolymerized C 5 diene content≤2% in the insulation polymeric kettle; Make the polymer fluid water cooler 9 of flowing through with insulation polymeric kettle recycle pump 8, after the cooling, a part is delivered to catalyzer still 2 with the preparation catalyzer; A part is returned insulation polymeric kettle 7 with control reaction temperature, and all the other deliver to the washing unit;
(4) alkali cleaning: be that the buck of 50 ℃ mass percent concentration 2% gets in first mixed flow device 10 and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 5: 1; Get into buck sedimentation tower 11 middle parts then, the height of buck sedimentation tower 11 is 12 meters, polymerization liquid and buck in buck sedimentation tower 11 through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(5) washing: second the mixed flow device 12 of water entering that is 50 ℃ by polymer resin liquid I and the temperature of buck sedimentation tower 11 cat head extraction; The volume ratio of polymer resin liquid I and water 5: 1 is mixed in second mixed flow device 12, gets into clear water sedimentation tower 13 middle parts then; The height of clear water sedimentation tower 13 is 12 meters; Through layering, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II:
(6) ammonia scrubbing: the ammoniacal liquor resin liquid of the mass percent concentration 0.4% that is 50 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation tower 13 cat head extraction gets into the 3rd mixed flow device 14; The volume ratio of polymer resin liquid II and water 5: 1 is mixed in the 3rd mixed flow device 14, gets into the middle part of ammoniacal liquor sedimentation tower 15 then; The height of ammoniacal liquor sedimentation tower 15 is 12 meters; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
Said polymer resin liquid III sedimentation after drying, moulding in the sedimentation storage tank make C 5 petroleum resin.
Claims (7)
1. the continuous washing method in the C 5 petroleum resin production process is characterized in that, said method comprising the steps of:
(1) alkali cleaning: be that the buck of 40～55 ℃ mass percent concentration 2% gets in first mixed flow device and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 4～6: 1, gets into buck sedimentation tower middle part then, polymerization liquid and buck in buck sedimentation tower through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(2) washing: second the mixed flow device of water entering that is 40～55 ℃ by polymer resin liquid I and the temperature of buck sedimentation column overhead extraction; The volume ratio 4～6: 1 of polymer resin liquid I and water; In second mixed flow device, mix, get into clear water sedimentation tower middle part then, through layering; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II;
(3) ammonia scrubbing: the ammoniacal liquor of the mass percent concentration 0.3%～0.5% that is 40～55 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation column overhead extraction gets into the 3rd mixed flow device; The volume ratio 4～6: 1 of polymer resin liquid II and ammoniacal liquor; In the 3rd mixed flow device, mix, get into ammoniacal liquor sedimentation tower middle part then, by discharging waste water at the bottom of the tower; By cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
2. continuous washing method as claimed in claim 1 is characterized in that, the temperature of said (1) alkali cleaning, (2) washing and (3) ammonia scrubbing step is 47～53 ℃.
3. continuous washing method as claimed in claim 1 is characterized in that, said buck is the aqueous solution of sodium hydroxide.
4. continuous washing method as claimed in claim 1 is characterized in that, the height of said buck sedimentation tower, clear water sedimentation tower and ammoniacal liquor sedimentation tower is respectively 5～20 meters.
5. the continuous production method of a C 5 petroleum resin is characterized in that, said method comprising the steps of:
(1) catalyzer preformulation: with nitrogen the catalyzer aluminum trichloride (anhydrous) is pressed in the catalyzer still, mixes through the refrigerative polymerization liquid with coming the self-heat conserving polymeric kettle, the quality of said aluminum trichloride (anhydrous) is 1% of a polymerization liquid quality;
(2) polyreaction: the mixed solution in the catalyzer still is delivered to polymerization reaction kettle with catalyst pump; Simultaneously the decylization cracked C 5 fraction is added in the polymerization reaction kettle; Temperature of reaction is controlled at 65～75 ℃; The adding weight of catalyzer aluminum trichloride (anhydrous) adds 0.3%～0.35% of weight for the decylization cracked C 5 fraction, and unpolymerized C 5 diene content is 13wt%～17wt% to the adding speed of control decylization cracked C 5 fraction in the polymerization reaction kettle to keep;
(3) insulation polymerization: the polymer fluid in the polymerization reaction kettle is delivered to the insulation polymeric kettle through water cooler with the reaction kettle recycle pump; The temperature of insulation polymeric kettle is controlled at 65～75 ℃; The transfer rate of controlled polymerization liquid makes the unpolymerized C 5 diene content≤2wt% in the insulation polymeric kettle; With insulation polymeric kettle recycle pump partially polymerized liquid is delivered to the catalyzer still with the preparation catalyzer after cooling, all the other deliver to the washing unit;
(4) alkali cleaning: be that the buck of 40～55 ℃ mass percent concentration 2% gets in first mixed flow device and mixes from the polymerization liquid and the temperature of the unitary decylization cracked C 5 fraction of polyreaction; The volume ratio of polymerization liquid and buck is 4～6: 1, gets into buck sedimentation tower middle part then, polymerization liquid and buck in buck sedimentation tower through layering; Water moves downward; Oil phase moves upward, by discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid I;
(5) washing: second the mixed flow device of water entering that is 40～55 ℃ by polymer resin liquid I and the temperature of buck sedimentation column overhead extraction; The volume ratio 4～6: 1 of polymer resin liquid I and water; In second mixed flow device, mix, get into clear water sedimentation tower then, through layering; By discharging waste water at the bottom of the tower, by cat head extraction polymer resin liquid II;
(6) ammonia scrubbing: the ammoniacal liquor resin liquid of the mass percent concentration 0.3%～0.5% that is 40～55 ℃ by the polymer resin liquid II and the temperature of clear water sedimentation column overhead extraction gets into the 3rd mixed flow device; The volume ratio 4～6: 1 of polymer resin liquid II and water; In the 3rd mixed flow device, mix, get into ammoniacal liquor sedimentation tower then, by discharging waste water at the bottom of the tower; By cat head extraction polymer resin liquid III, polymer resin liquid III delivers to the sedimentation storage tank.
6. the continuous production method of C 5 petroleum resin as claimed in claim 4 is characterized in that, said polymer resin liquid III sedimentation after drying, moulding in the sedimentation storage tank make C 5 petroleum resin.
7. the continuous production method of C 5 petroleum resin as claimed in claim 4 is characterized in that, said decylization cracked C 5 fraction is the cut after cracked C 5 fraction removes cyclopentadiene and NSC 7352, or further removes the cut behind the isoprene.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117304404A (en) * | 2023-11-28 | 2023-12-29 | 上海班德路橡胶科技有限公司 | Method and device for treating liquid carbon five petroleum resin polymerization liquid |
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| CN1158865A (en) * | 1996-03-05 | 1997-09-10 | 中国科学院成都有机化学研究所 | Processing method of carbon-5 fraction cation polymerization liquid |
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| US4173699A (en) * | 1977-03-11 | 1979-11-06 | Ato Chimie | Process for manufacturing petroleum resins for adhesive thermofusible compositions |
| JPS57195715A (en) * | 1981-05-28 | 1982-12-01 | Toyo Soda Mfg Co Ltd | Production of petroleum resin |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117304404A (en) * | 2023-11-28 | 2023-12-29 | 上海班德路橡胶科技有限公司 | Method and device for treating liquid carbon five petroleum resin polymerization liquid |
| CN117304404B (en) * | 2023-11-28 | 2024-02-09 | 上海班德路橡胶科技有限公司 | Method and device for treating liquid carbon five petroleum resin polymerization liquid |
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Application publication date: 20120620 |