CN114195913B - Method for improving flash evaporation effect of carbon five petroleum resin - Google Patents
Method for improving flash evaporation effect of carbon five petroleum resin Download PDFInfo
- Publication number
- CN114195913B CN114195913B CN202111589198.8A CN202111589198A CN114195913B CN 114195913 B CN114195913 B CN 114195913B CN 202111589198 A CN202111589198 A CN 202111589198A CN 114195913 B CN114195913 B CN 114195913B
- Authority
- CN
- China
- Prior art keywords
- tower
- flash
- carbon
- petroleum resin
- liquid
- 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.)
- Active
Links
Classifications
-
- 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
- C08F6/00—Post-polymerisation treatments
- C08F6/001—Removal of residual monomers by physical means
- C08F6/003—Removal of residual monomers by physical means from polymer solutions, suspensions, dispersions or emulsions without recovery of the polymer therefrom
-
- 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
- C08F6/00—Post-polymerisation treatments
- C08F6/06—Treatment of polymer solutions
- C08F6/10—Removal of volatile materials, e.g. solvents
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a method for improving the flash evaporation effect of carbon five petroleum resin, belongs to the technical field of carbon five petroleum resin processing, and mainly solves the problem of poor flash evaporation effect in the prior art. Specifically, the carbon five petroleum resin polymerization liquid subjected to primary flash evaporation is preheated by a feed preheater and then enters a second flash evaporation tower for flash evaporation, light components are discharged and condensed through the top of the second flash evaporation tower, the carbon five petroleum resin liquid in the tower kettle continuously enters a third flash evaporation tower for flash evaporation, liquid resin with small molecular weight is discharged and condensed through the top of the third flash evaporation tower, and the carbon five petroleum resin liquid in the tower kettle is discharged through a tower kettle extraction pump and enters the subsequent process. The invention can effectively improve the flash evaporation effect of the carbon five petroleum resin, increase the adjustment method of the softening point, improve the quality of the carbon five petroleum resin and achieve the maximum recycling of energy.
Description
Technical Field
The invention relates to the technical field of carbon five petroleum resin processing, in particular to a method for improving the flash evaporation effect of carbon five petroleum resin.
Background
The carbon five petroleum resin is used as a main product extremely represented in the carbon five comprehensive utilization project, and has the advantages of simple synthesis, low price, good alkali resistance, water resistance, weather resistance, good compatibility with organic matters and the like, so that the carbon five petroleum resin is increasingly widely used.
The process for synthesizing the carbon five petroleum resin is generally as follows: firstly, pretreating a carbon five raw material to enable CPD in the carbon five raw material to be thermally dimerized to form DCPD, then polymerizing a carbon five fraction in a solvent by taking Lewis acid as a catalyst, and then washing a reaction polymerization liquid to remove the catalyst. And distilling the polymerization solution to remove unreacted light components such as carbon five and solvent, and then distilling under reduced pressure to remove oligomer (namely liquid resin) to obtain the carbon five petroleum resin.
In the process of removing unpolymerized carbon five, solvent and liquid resin from the polymerized liquid of carbon five petroleum resin, a falling film evaporator and other devices are generally adopted to realize the reduced pressure distillation removal. In the continuous production process, the resin polymerization liquid continuously enters a distillation device, the corresponding light components are separated from the top, and the relatively pure carbon five petroleum resin is discharged from the bottom of the device. When a certain link in the production process fluctuates, the associated light components cannot be completely removed and directly brought into the next process, and the index of the petroleum resin is irrevocably abnormal, such as low softening point, large color, large odor with the light components and the like, so that the quality of the carbon five petroleum resin is seriously affected. In severe cases, the resin liquid has low viscosity and thin morphology, and the resin pelletization step cannot complete pelletization packaging.
Disclosure of Invention
The invention aims to provide a method for improving the flash evaporation effect of carbon five petroleum resin. The flash evaporation effect of the carbon five petroleum resin can be effectively improved, the adjustment method of the softening point of the carbon five petroleum resin is increased, the quality of the carbon five petroleum resin is improved, and the maximum recycling of energy sources is achieved.
The technical scheme of the invention is as follows: a method for improving the flash effect of carbon five petroleum resin, the carbon five petroleum resin polymeric liquid after primary flash evaporation is preheated by a feed preheater and then enters a second flash evaporation tower for flash evaporation, the light components are discharged and condensed from the top of the second flash evaporation tower, the carbon five petroleum resin liquid in the tower kettle is continuously introduced into a third flash evaporation tower for flash evaporation, the liquid resin with small molecular weight is discharged and condensed from the top of the third flash evaporation tower, and the carbon five petroleum resin liquid in the tower kettle is discharged by a tower kettle extraction pump.
When the flash evaporation effect needs to be improved, a kettle liquid return pipeline is arranged at the discharge outlet of the third flash evaporation tower kettle, the kettle liquid return pipeline comprises a kettle liquid return pump and two kettle liquid return branch pipes which are connected with the output outlet of the kettle liquid return pump and are arranged in parallel, one kettle liquid return branch pipe is connected with the feed inlet of the second flash evaporation tower, the carbon five petroleum resin liquid is returned to the second flash evaporation tower to continue flash evaporation treatment, namely, large circulation flash evaporation, the other kettle liquid return branch pipe is connected with the feed inlet of the third flash evaporation tower, the carbon five petroleum resin liquid is returned to the third flash evaporation tower to perform flash evaporation treatment, namely, small circulation flash evaporation, and the carbon five petroleum resin liquid can be returned to the second flash evaporation tower or the third flash evaporation tower to be treated according to the condition of the carbon five petroleum resin liquid, so that the circulation multiple flash evaporation of the carbon five petroleum resin is realized.
In the invention, if the circulation is selected to be carried out for multiple flash evaporation, the circulation time is 2-12 hours.
In the invention, the pressure in the second flash distillation tower is larger than that in the third flash distillation tower. As one embodiment, the control range of the pressure in the second flash tower is-40 to-60 KPa, and the control value of the pressure in the third flash tower is the ultimate vacuum degree.
In the invention, the feeding flow of the feeding preheater of the second flash tower is 7-11m 3 And/h, the tube side medium is a carbon five petroleum resin polymer liquid, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 250-280 ℃.
In the invention, the resin liquid level in the tower bottom of the second flash distillation tower is 40-60%, and the light components in the carbon five petroleum resin are removed from the tower top. The resin liquid level in the third flash distillation tower kettle is 40-60%, and the liquid resin with small molecular weight in the carbon five petroleum resin is removed from the tower top.
As an embodiment of the invention, the second flash tower and the third flash tower are not provided with vertical falling film evaporators, but are provided with steam distributors connected with a steam source in the respective tower kettles for providing stripping steam in the towers. In the process, the steam flow provided by the steam distributor is 60-70 kg/h, and the steam pressure range is 1.4-1.6 MPa. The adopted flash tower is not provided with a vertical falling film evaporator, so that the flash space inside the flash tower is enlarged, and the flash effect is improved. The steam heating can be adopted to vaporize the petroleum fraction at a lower boiling point, so that the light component in the liquid phase below the feeding section is vaporized, the light component content in the resin liquid in the tower kettle is reduced, and the light component extraction rate and flash evaporation removal effect are further improved.
In the invention, the kettle liquid return pump and the tower kettle extraction pump are variable-frequency screw pumps, and the variable-frequency is 30-40Hz.
Compared with the prior art, the invention has the advantages that:
1. the method for improving the flash evaporation effect of the carbon five petroleum resin solves the technical defects that the quality of the carbon five petroleum resin is affected and the like because light components are not removed cleanly in the flash evaporation process in the carbon five petroleum resin device, and provides a method for improving the flash evaporation effect of the carbon five petroleum resin, increasing the softening point of the carbon five petroleum resin and other adjustment methods, improving the quality of the carbon five petroleum resin and achieving the maximum recycling of energy.
2. The resin polymerization liquid in the invention enters the second flash tower after being heated at high temperature by the feeding preheater, so that light components such as solvent and the like can be quickly gasified and separated, the feeding preheater preheats the resin polymerization liquid by using high-pressure high-temperature steam, and enough temperature is provided for the resin polymerization liquid to remove the light components, thereby ensuring the flash evaporation effect.
3. According to the method for improving the flash evaporation effect of the carbon five petroleum resin, provided by the invention, the flash evaporation removal effect of light components in the petroleum resin is greatly ensured by quantitatively inputting the stripping steam in the flash evaporation tower.
4. According to the method for improving the flash evaporation effect of the carbon five petroleum resin, the kettle liquid return pipeline is arranged at the tail end of the working procedure, and the small-cycle flash evaporation and the large-cycle flash evaporation can be selected according to the quality index degree of the carbon five petroleum resin, so that the requirements of different situations are met, and the diversity and the flexibility of the operation adjustment method are reflected.
5. According to the method for improving the flash evaporation effect of the carbon five petroleum resin, provided by the invention, the kettle liquid return pump and the tower kettle extraction pump are both variable-frequency screw pumps, so that the purpose of properly adjusting the frequency of the motor according to the quality index requirement of the carbon five petroleum resin can be achieved, and the energy can be effectively saved.
Drawings
FIG. 1 is a schematic diagram of the flash vaporization system of the present invention.
FIG. 2 is a cross-sectional view of the bottom of the flash column of the present invention.
Wherein: 1-a feed preheater, 2-a second flash tower, 3-a second flash tower condenser, 4-a second tower kettle extraction pump, 5-a third flash tower, 6-a kettle liquid return pump, 7-a first return valve, 8-a second return valve, 9-a third flash tower condenser, 10-a third tower kettle extraction pump and 12-a steam distributor.
Detailed Description
The invention will be further described with reference to specific embodiments in the drawings.
As shown in fig. 1, a flash system for use in an embodiment of the present invention includes a feed preheater 1, a second flash column 2, and a third flash column 5. The second flash tower feeding preheater 1 is connected with the second flash tower 2, and a tower kettle discharge port of the second flash tower 2 is connected with the third flash tower 5 through a second tower kettle extraction pump 4. The top gas outlet of the second flash tower 2 is connected with a second flash tower condenser 3, and the liquid outlet of the second flash tower condenser 3 is connected with a storage tank. The top gas outlet of the third flash tower 5 is connected with a third flash tower condenser 9, and the liquid outlet of the third flash tower condenser 9 is connected with a storage tank. And a discharge hole of the third flash tower 5 is connected with a third tower kettle extraction pump 10. The second flash tower 2 and the third flash tower 5 are respectively connected with a vacuum pump. The vacuum pump is an oil-free vertical vacuum pump, and the corresponding ultimate vacuum degree (gauge pressure) is-96 to-98 KPa.
The discharge outlet of the tower kettle of the third flash tower 5 is provided with a kettle liquid return pipeline which comprises a kettle liquid return pump 6 and two paths of kettle liquid return branch pipes which are connected with the output port of the kettle liquid return pump 6 and are connected in parallel. One path of kettle liquid return branch pipe is connected with a feed inlet of the second flash tower 2, a first return valve 7 is arranged, and the carbon five petroleum resin liquid is returned to the second flash tower 2 for continuous flash evaporation treatment, namely large circulation flash evaporation; the other path of kettle liquid return branch pipe is connected with the feed inlet of the third flash tower 5 and is provided with a second return valve 8, and the carbon five petroleum resin liquid is returned to the third flash tower 5 for flash evaporation treatment, namely small circulation flash evaporation. In the process, whether the carbon five petroleum resin liquid is returned to the second flash tower 2 or the third flash tower 5 for treatment can be selected according to the condition of the carbon five petroleum resin liquid, and the circulating multiple flash evaporation of the carbon five petroleum resin can be realized.
The second flash tower 2 and the third flash tower 5 are not provided with vertical falling film evaporators, but are provided with steam distributors 12 connected with a steam source in the respective tower kettles. The main body of the steam distributor 12 is an annular steam pipe, and the annular steam pipe is connected with a straight pipe which extends out of the flash tower and is connected with a steam supply device. The annular steam pipe is provided with a steam hole towards the upward side, and steam is sprayed upwards from the steam hole to heat materials in the tower.
Example 1
1) The carbon five petroleum resin polymerization liquid after primary flash evaporation enters a feed preheater 1 to be heated, and the feed flow is 7m 3 And/h, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 250 ℃. The heated resin polymerization liquid enters a second flash tower 2 for flash evaporation, the pressure in the tower is-50 KPa, the stripping steam is 60kg/h, and the light components are removed by condensation of a second flash tower condenser 3.
2) And the resin liquid in the tower kettle of the second flash evaporation tower is fed into a third flash evaporation tower 5 for flash evaporation through a second tower kettle extraction pump 4, and the liquid level of the resin liquid in the tower kettle of the second flash evaporation tower is controlled to be 40-60%. The pressure in the third flash tower 5 is extreme vacuum, stripping steam is 60kg/h, the liquid resin with small molecular weight is condensed and removed by the third flash tower condenser 9, the liquid level of the tower kettle is controlled to be 40-60%, and qualified carbon five petroleum resin liquid is fed into the granulating process by the tower kettle extraction pump 10, and the pump frequency of the machine is 30-40Hz.
3) If the softening point of the tail end of the carbon five petroleum resin is 82 ℃ and the hue No. 4 is larger, the removal of the light components is judged to be incomplete, and the flash evaporation effect needs to be improved. And starting the kettle liquid return pump 6, opening the first return valve 7, and circularly returning the carbon five petroleum resin to the second flash tower 2 for flash evaporation in the state that the second return valve 8 is closed at the moment, so as to implement large-cycle flash evaporation operation. The frequency of the kettle liquid return pump 6 is 40Hz. After 12 hours of cyclic flash evaporation, the resin has a softening point of 99 ℃ and a hue of No. 3 and is odorless.
In the process, the steam pressure to the second flash column 2 and the third flash column 5 is in the range of 1.4 to 1.6MPa.
Example 2
1) The carbon five petroleum resin polymerization liquid after primary flash evaporation enters a feed preheater 1 to be heated, and the feed flow is 8m 3 And/h, the shell side medium is steam with the pressure more than or equal to 4.0MPa,the heating temperature was 260 ℃. The heated resin polymerization liquid enters a second flash tower 2 for flash evaporation, the pressure in the tower is-45 KPa, the stripping steam is 60kg/h, and the light components are removed by condensation of a second flash tower condenser 3.
2) Resin liquid in the tower kettle of the second flash tower 2 is fed into the third flash tower 5 for flash evaporation through the second tower kettle extraction pump 4, and meanwhile, the liquid level of the resin liquid in the tower kettle of the second flash tower is controlled to be 40-60%. The pressure in the third flash tower 5 is extreme vacuum, stripping steam is 60kg/h, the liquid resin with small molecular weight is condensed and removed by the third flash tower condenser 9, the liquid level of the tower kettle is controlled to be 40-60%, and qualified carbon five petroleum resin liquid is fed into the granulating process by the tower kettle extraction pump 10, and the pump frequency of the machine is 30-40Hz.
3) If the softening point of the tail end of the carbon five petroleum resin is 82 ℃ and the hue No. 4 is larger, the removal of the light components is judged to be incomplete, and the flash evaporation effect needs to be improved. And starting the kettle liquid return pump 6, opening the first return valve 7, and circularly returning the carbon five petroleum resin to the second flash tower 2 for flash evaporation in the state that the second return valve 8 is closed at the moment, so as to implement large-cycle flash evaporation operation. The frequency of the kettle liquid return pump 6 is 40Hz. After 8 hours of cyclic flash evaporation, the resin had a softening point of 96.5 ℃ and a hue of No. 4, and was slightly odorous.
In the process, the steam pressure of the second flash tower 2 and the third flash tower 5 ranges from 1.4 MPa to 1.6MPa.
Example 3
1) The polymerization liquid of the carbon five petroleum resin enters a feeding preheater 1 to be heated, and the feeding flow is 7m 3 And/h, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 280 ℃. The heated resin polymerization liquid enters a second flash tower 2 for flash evaporation, the pressure in the tower is-50 KPa, the stripping steam is 65kg/h, and the light components are removed by condensation of a second flash tower condenser 3.
2) The liquid level of resin liquid in the tower kettle of the second flash distillation tower is controlled to be 40-60%, the resin liquid is fed into the third flash distillation tower 5 for flash distillation through the second tower kettle extraction pump 4, the pressure in the tower is extreme vacuum, the stripping steam is 65kg/h, the liquid resin with small molecular weight is condensed and removed through the third flash distillation tower condenser 9, the liquid level of the tower kettle is controlled to be 40-60%, and qualified carbon five petroleum resin liquid is fed into the granulating process through the tower kettle extraction pump 10, and the pump frequency is 30-40Hz.
3) If the softening point of the tail end of the carbon five petroleum resin is 82 ℃ and the hue No. 4 is larger, the removal of the light components is judged to be incomplete, and the flash evaporation effect needs to be improved. And starting the kettle liquid return pump 6, opening the first return valve 7, and circularly returning the carbon five petroleum resin to the second flash tower 2 for flash evaporation in the state that the second return valve 8 is closed at the moment, so as to implement large-cycle flash evaporation operation. The frequency of the kettle liquid return pump 6 is 40Hz. After 4 hours of cyclic flash evaporation, the resin had a softening point of 92.5 ℃ and a hue of No. 4 and was odorous.
In the process, the steam pressure of the second flash tower 2 and the third flash tower 5 ranges from 1.4 MPa to 1.6MPa.
Example 4
1) The polymerization liquid of the carbon five petroleum resin enters a feeding preheater 1 to be heated, and the feeding flow is 7m 3 And/h, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 270 ℃. The heated resin polymerization liquid enters a second flash tower 2 for flash evaporation, the pressure in the tower is-50 KPa, the stripping steam is 70kg/h, and the light components are removed by condensation of a second flash tower condenser 3.
2) The liquid level of resin liquid in the tower kettle of the second flash distillation tower is controlled to be 40-60%, the resin liquid is fed into the third flash distillation tower 5 for flash distillation through the second tower kettle extraction pump 4, the pressure in the tower is extreme vacuum, the stripping steam is 70kg/h, the liquid resin with small molecular weight is condensed and removed through the third flash distillation tower condenser 9, the liquid level of the tower kettle is controlled to be 40-60%, and qualified carbon five petroleum resin liquid is fed into the granulating process through the tower kettle extraction pump 10, and the pump frequency is 30-40Hz.
3) If the softening point of the tail end of the carbon five petroleum resin is 82 ℃ and the hue No. 4 is larger, the removal of the light components is judged to be incomplete, and the flash evaporation effect needs to be improved. And starting the kettle liquid return pump 6, opening the first return valve 7, and circularly returning the carbon five petroleum resin to the second flash tower 2 for flash evaporation in the state that the second return valve 8 is closed at the moment, so as to implement large-cycle flash evaporation operation. The frequency of the kettle liquid return pump 6 is 40Hz. After 2 hours of cyclic flash evaporation, the softening point of the resin was 90.5 ℃, the hue 4 was reduced, and the odor was decreased.
In the process, the steam pressure of the second flash tower 2 and the third flash tower 5 ranges from 1.4 MPa to 1.6MPa.
Example 5
1) The polymerization liquid of the carbon five petroleum resin enters a feeding preheater 1 to be heated, and the feeding flow is 7m 3 And/h, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 250 ℃. The heated resin polymerization liquid enters a second flash tower 2 for flash evaporation, the pressure in the tower is-50 KPa, the stripping steam is 60kg/h, and the light components are removed by condensation of a second flash tower condenser 3.
2) The liquid level of resin liquid in the tower kettle of the second flash tower 2 is controlled to be 40-60%, the resin liquid is fed into the third flash tower 5 for flash evaporation through the second tower kettle extraction pump 4, the pressure in the tower is extreme vacuum, the stripping steam is 60kg/h, the liquid resin with small molecular weight is condensed and removed through the third flash tower condenser 9, the liquid level of the tower kettle is controlled to be 40-60%, and qualified carbon five petroleum resin liquid is fed into the granulating process through the tower kettle extraction pump 10, and the pump frequency is 30-40Hz.
3) If the softening point of the tail end of the carbon five petroleum resin is detected to be 99 ℃, the hue is No. 3, and the light component is judged to be incompletely removed, and the flash evaporation effect needs to be improved. And starting the kettle liquid return pump 6, opening the second return valve 8, and circularly returning the carbon five petroleum resin to the second flash tower 3 for flash evaporation in the state that the first return valve 7 is closed at the moment, so as to implement small-cycle flash evaporation operation. The frequency of the kettle liquid return pump 6 is 40Hz. After 4 hours of cyclic flash evaporation, the resin has a softening point of 100 ℃, a hue of No. 3 and no smell.
In the process, the steam pressure of the second flash tower 2 and the third flash tower 5 ranges from 1.4 MPa to 1.6MPa.
The foregoing is merely a preferred embodiment of the present invention, and it should be noted that modifications and improvements can be made by those skilled in the art without departing from the structure of the present invention, and these do not affect the effect of the implementation of the present invention and the utility of the patent.
Claims (6)
1. A method for improving the flash vaporization effect of the carbon five petroleum resin is characterized in that carbon five petroleum resin polymerization liquid subjected to primary flash vaporization enters a second flash vaporization tower for flash vaporization after being preheated by a feed preheater, light components are discharged and condensed from the top of the second flash vaporization tower, carbon five petroleum resin liquid in a tower kettle continuously enters a third flash vaporization tower for flash vaporization, liquid resin with small molecular weight is discharged and condensed from the top of the third flash vaporization tower, and the carbon five petroleum resin liquid in the tower kettle is discharged by a tower kettle discharge pump to enter the subsequent process;
the discharge port of the third flash distillation tower kettle is provided with a kettle liquid return pipeline which comprises a kettle liquid return pump and two kettle liquid return branch pipes which are connected with the output port of the kettle liquid return pump and are arranged in parallel, one kettle liquid return branch pipe is connected with the feed inlet of the second flash distillation tower, and the carbon five petroleum resin liquid is returned to the second flash distillation tower to continue the flash distillation treatment; the other path of kettle liquid return branch pipe is connected with the feed inlet of the third flash tower, and returns the carbon five petroleum resin liquid to the third flash tower for flash evaporation treatment, and the carbon five petroleum resin liquid is selectively returned to the second flash tower or the third flash tower for treatment according to the condition of the carbon five petroleum resin liquid, so that the carbon five petroleum resin is circularly and repeatedly flashed; the circulation time is 2-12 hours when the flash evaporation is carried out for a plurality of times in a circulation way;
the feed flow of the feed preheater of the second flash column is 7-11m 3 And/h, the tube side medium is a carbon five petroleum resin polymer liquid, the shell side medium is steam with the pressure of more than or equal to 4.0MPa, and the heating temperature is 250-280 ℃;
the resin liquid level in the tower kettle of the second flash distillation tower is 40-60%; the resin liquid level in the third flash distillation tower kettle is 40-60%.
2. The method for improving the flash effect of a carbon five petroleum resin according to claim 1, wherein the pressure in the second flash column is greater than the pressure in the third flash column.
3. The method for improving the flash vaporization effect of the carbon five petroleum resin according to claim 2, wherein the control range of the pressure in the second flash distillation tower is-40 to-60 KPa, and the control value of the pressure in the third flash distillation tower is the ultimate vacuum degree.
4. The method for improving the flash vaporization effect of the carbon five petroleum resin according to claim 1, wherein the second flash vaporization tower and the third flash vaporization tower are not provided with vertical falling film evaporators, but are provided with steam distributors connected with steam sources in the respective tower kettles, the steam flow provided by the steam distributors is 60-70 kg/h, and the steam pressure ranges from 1.4 MPa to 1.6MPa.
5. The method for improving the flash vaporization effect of the carbon five petroleum resin according to claim 1, wherein the tank liquor return pump and the tower bottom extraction pump are screw pumps.
6. The method for improving the flash vaporization effect of the carbon five petroleum resin according to claim 5, wherein the pump frequency of the tank liquor return pump and the tank liquor extraction pump is 30-40Hz.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111589198.8A CN114195913B (en) | 2021-12-23 | 2021-12-23 | Method for improving flash evaporation effect of carbon five petroleum resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111589198.8A CN114195913B (en) | 2021-12-23 | 2021-12-23 | Method for improving flash evaporation effect of carbon five petroleum resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114195913A CN114195913A (en) | 2022-03-18 |
| CN114195913B true CN114195913B (en) | 2023-08-18 |
Family
ID=80656146
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111589198.8A Active CN114195913B (en) | 2021-12-23 | 2021-12-23 | Method for improving flash evaporation effect of carbon five petroleum resin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114195913B (en) |
Citations (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4439601A (en) * | 1979-03-30 | 1984-03-27 | Cosden Technology, Inc. | Multiple stage devolatilization process for mass processable polymers |
| WO1995035326A1 (en) * | 1994-06-17 | 1995-12-28 | Exxon Chemical Patents Inc. | Prestripped polymer used to improve koch reaction dispersant additives |
| CN1193629A (en) * | 1997-01-08 | 1998-09-23 | 北京燕山石油化工公司研究院 | Concentrating method of polymer solution |
| CN1214341A (en) * | 1997-10-15 | 1999-04-21 | 北京燕山石油化工公司研究院 | Method for removal of volatile component from polymer solution |
| US6365006B1 (en) * | 1997-10-01 | 2002-04-02 | General Electric Company | Method for distilling a mixture of substances and device for realizing the same |
| CN1694758A (en) * | 2002-09-16 | 2005-11-09 | 切夫里昂菲利普化学有限责任公司 | Process and system for removing heavies from diluent recycled to a slurry polymerization reactor |
| CN101538349A (en) * | 2008-03-18 | 2009-09-23 | 大庆华科股份有限公司 | Process and equipment for continuous catalytic polymerization aggregation of C9 petroleum resin |
| CN204121793U (en) * | 2014-09-24 | 2015-01-28 | 淄博鲁华同方化工有限公司 | A kind of C5 Petropols remove the device of light component |
| CN104592507A (en) * | 2015-02-12 | 2015-05-06 | 吉林众鑫化工集团有限公司 | Method for continuously producing macromolecular unsaturated polyether |
| CN105418849A (en) * | 2014-09-19 | 2016-03-23 | 上海宝钢化工有限公司 | Production method for high-softening-point coumarone resin |
| US9340481B1 (en) * | 2014-11-14 | 2016-05-17 | Celanese International Corporation | Process for flashing a reaction medium comprising lithium acetate |
| CN106232197A (en) * | 2014-05-23 | 2016-12-14 | 株式会社神户制钢所 | Distilling apparatus |
| CN108148608A (en) * | 2016-12-06 | 2018-06-12 | 何巨堂 | With the rapidly pre-warming series connection thermophilic pyrolysis hydrocarbon material method for pyrolysis of formula of Two-way Cycle powder |
| CN210314086U (en) * | 2019-06-25 | 2020-04-14 | 安徽同心新材料科技有限公司 | Catalyst desorption system for C5 petroleum resin production |
| CN111699202A (en) * | 2017-12-04 | 2020-09-22 | 北欧化工股份公司 | Method for recovering olefin in solution polymerization process |
| CN111961496A (en) * | 2020-09-04 | 2020-11-20 | 中冶焦耐(大连)工程技术有限公司 | Production process and system for modifying asphalt by multi-reaction-kettle parallel tubular furnace heating method |
| CN112812233A (en) * | 2021-01-08 | 2021-05-18 | 淄博鲁华泓锦新材料股份有限公司 | Continuous production process of carbon five-resin |
| CN215049940U (en) * | 2021-03-26 | 2021-12-07 | 广东新华粤树脂科技有限公司 | Carbon five-carbon nine-copolymerization petroleum resin non-polymerized mixture carbon five-separation device |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7524904B2 (en) * | 2002-09-16 | 2009-04-28 | Chevron Phillips Chemical Company Lp | Process and apparatus for separating polymer solids, hydrocarbon fluids, and purge gas |
| BRPI0314396B1 (en) * | 2002-09-16 | 2015-09-01 | Chevron Phillips Chemical Co | Suspension polymerization liquid recovery and purification system |
| US20170151507A1 (en) * | 2015-12-01 | 2017-06-01 | Kuwait Institute For Scientific Research | Combination multi-effect distillation and multi-stage flash evaporation system |
| US10570224B2 (en) * | 2016-04-15 | 2020-02-25 | Exxonmobil Chemical Patents Inc. | Polymerization using a stripping agent for devolatilization |
-
2021
- 2021-12-23 CN CN202111589198.8A patent/CN114195913B/en active Active
Patent Citations (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4439601A (en) * | 1979-03-30 | 1984-03-27 | Cosden Technology, Inc. | Multiple stage devolatilization process for mass processable polymers |
| WO1995035326A1 (en) * | 1994-06-17 | 1995-12-28 | Exxon Chemical Patents Inc. | Prestripped polymer used to improve koch reaction dispersant additives |
| CN1193629A (en) * | 1997-01-08 | 1998-09-23 | 北京燕山石油化工公司研究院 | Concentrating method of polymer solution |
| US6365006B1 (en) * | 1997-10-01 | 2002-04-02 | General Electric Company | Method for distilling a mixture of substances and device for realizing the same |
| CN1214341A (en) * | 1997-10-15 | 1999-04-21 | 北京燕山石油化工公司研究院 | Method for removal of volatile component from polymer solution |
| CN1694758A (en) * | 2002-09-16 | 2005-11-09 | 切夫里昂菲利普化学有限责任公司 | Process and system for removing heavies from diluent recycled to a slurry polymerization reactor |
| CN101538349A (en) * | 2008-03-18 | 2009-09-23 | 大庆华科股份有限公司 | Process and equipment for continuous catalytic polymerization aggregation of C9 petroleum resin |
| CN106232197A (en) * | 2014-05-23 | 2016-12-14 | 株式会社神户制钢所 | Distilling apparatus |
| CN105418849A (en) * | 2014-09-19 | 2016-03-23 | 上海宝钢化工有限公司 | Production method for high-softening-point coumarone resin |
| CN204121793U (en) * | 2014-09-24 | 2015-01-28 | 淄博鲁华同方化工有限公司 | A kind of C5 Petropols remove the device of light component |
| US9340481B1 (en) * | 2014-11-14 | 2016-05-17 | Celanese International Corporation | Process for flashing a reaction medium comprising lithium acetate |
| CN104592507A (en) * | 2015-02-12 | 2015-05-06 | 吉林众鑫化工集团有限公司 | Method for continuously producing macromolecular unsaturated polyether |
| CN108148608A (en) * | 2016-12-06 | 2018-06-12 | 何巨堂 | With the rapidly pre-warming series connection thermophilic pyrolysis hydrocarbon material method for pyrolysis of formula of Two-way Cycle powder |
| CN111699202A (en) * | 2017-12-04 | 2020-09-22 | 北欧化工股份公司 | Method for recovering olefin in solution polymerization process |
| CN210314086U (en) * | 2019-06-25 | 2020-04-14 | 安徽同心新材料科技有限公司 | Catalyst desorption system for C5 petroleum resin production |
| CN111961496A (en) * | 2020-09-04 | 2020-11-20 | 中冶焦耐(大连)工程技术有限公司 | Production process and system for modifying asphalt by multi-reaction-kettle parallel tubular furnace heating method |
| CN112812233A (en) * | 2021-01-08 | 2021-05-18 | 淄博鲁华泓锦新材料股份有限公司 | Continuous production process of carbon five-resin |
| CN215049940U (en) * | 2021-03-26 | 2021-12-07 | 广东新华粤树脂科技有限公司 | Carbon five-carbon nine-copolymerization petroleum resin non-polymerized mixture carbon five-separation device |
Non-Patent Citations (1)
| Title |
|---|
| 张和平等主编.现代乳品工业手册.中国轻工业出版社,2005,第391-395页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114195913A (en) | 2022-03-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110498787B (en) | Lactide purification system and purification method | |
| CN102040676B (en) | Method for depriving solvent for cis-polybutadiene | |
| CN107739300A (en) | A kind of process for producing high-purity isobutene and ethylene glycol mono-tert-butyl ether | |
| CN111333530B (en) | Heat pump rectification process for recycling DMAC (dimethylacetamide) or DMF (dimethyl formamide) waste liquid | |
| CN103044598B (en) | Method for flash evaporating and concentrating of liquid ethylene propylene rubber | |
| WO2019090884A1 (en) | Polymerization process of impact polypropylene | |
| CN114195913B (en) | Method for improving flash evaporation effect of carbon five petroleum resin | |
| CN111621012A (en) | Polysulfone series resin polymerization dehydration process | |
| CN115010859B (en) | Method for producing carbon nine hydrogenated resin by recycling hot polymerization liquid resin | |
| CN204625414U (en) | A kind of five tower three-effect rectification systems of DMAC or DMF waste liquid | |
| CN101070283A (en) | Fatty-acid methyl ester producing process and apparatus | |
| CN115779472A (en) | Refining method and rectifying device for crude butanol in 1, 4-butanediol production | |
| CN112175112B (en) | Three-kettle coagulation method for solution polymerized butadiene styrene rubber | |
| KR101334397B1 (en) | Preparation method of dimer acid with high purity | |
| CN106397089B (en) | Method and system for recovering and purifying hexane solvent in ethylene propylene rubber production | |
| CN110694572A (en) | Equipment for degrading polytetrahydrofuran and recycling tetrahydrofuran and improved process | |
| CN114307212A (en) | Production method of three-stage continuous flash evaporation of carbon five petroleum resin | |
| CN103936601B (en) | ammonia recovery method in ethanolamine production | |
| CN112142876B (en) | Method for coagulating butadiene rubber solution | |
| CN115197345B (en) | Energy-saving method for coagulation process in synthetic rubber production | |
| CN112125988A (en) | Coagulation method for styrene thermoplastic elastomer solution | |
| CN112111026B (en) | Method for coagulating isoprene rubber solution | |
| CN217511866U (en) | Equipment for continuously producing styrene butadiene rubber | |
| CN112142877B (en) | Coagulation method for butadiene rubber solution | |
| CN221107018U (en) | System device for separating dimethylformamide solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 525000 Petrochemical Industrial Zone, Maoming City, Guangdong Province (Qijing section) Applicant after: Guangdong Luzhonghua New Material Co.,Ltd. Address before: 525000 Petrochemical Industrial Zone, Maoming City, Guangdong Province (Qijing section) Applicant before: MAOMING LUHUA NEW MATERIAL Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |