CN201459002U - Continuous propylene homopolymerization or copolymerization process device - Google Patents
Continuous propylene homopolymerization or copolymerization process device Download PDFInfo
- Publication number
- CN201459002U CN201459002U CN2009201107621U CN200920110762U CN201459002U CN 201459002 U CN201459002 U CN 201459002U CN 2009201107621 U CN2009201107621 U CN 2009201107621U CN 200920110762 U CN200920110762 U CN 200920110762U CN 201459002 U CN201459002 U CN 201459002U
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- propylene
- homopolymerization
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
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- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Polymerisation Methods In General (AREA)
Abstract
The utility model relates to a continuous propylene homopolymerization or copolymerization process device. A propylene input tube, a catalyst configuration tube, an aluminum triethyl input tube and an electron donor input tube are connected with an input port in the middle of a cannular prepolymerization reactor via an aluminum triethyl mixer. An output port on the lower part of the cannular prepolymerization reactor is connected with an input port on the lower part of a cannular homopolymerization reactor. An output port in the middle of the cannular homopolymerization reactor is connected with an input port in the middle of a supercritical copolymerization reactor. The output port on the lower part of the supercritical copolymerization reactor is connected with an input port on the lower part of a cannular copolymerization reactor. The output port on the lower part of the cannular copolymerization reactor is connected with a discharge tube. The bottom of the supercritical copolymerization reactor is communicated with the top of the supercritical copolymerization reactor by connecting a cooler and a propylene compressor through a pipeline. The process device has part of the characteristics of the Spheripol process and the borstar process, is flexible and diversified and has strong adaptability to the markets.
Description
Technical field
The utility model relates to continuous homopolymerization of a kind of propylene or copolymerization process device.
Background technology
One group or two groups placed in-line annular-pipe reactors of Spheripol process using are produced homopolymer polypropylene and random copolymers, and one or two Gas-phase reactor of connecting is again produced impact copolymer.
Spheripol technology is one of current most advanced reliable polymarization method for prodcing polyacrylates.Different with other technologies is, its catalyzer powder is spheroidal, and particle is big and evenly, some industrialized unit products have been realized directly dispatching from the factory without granulation, especially for high MFR can not extruder grain product.In addition, homopolymerization adopts the liquid phase annular-pipe reactor, and multiphase copolymer adopts vapor phase process dense fluidized bed bioreactor.
In order to utilize the bimodal molecular weight distribution of widening, also because plant construction needs two placed in-line annular-pipe reactors of the general employing of Spheripol technology on a large scale.Though this design investment is higher, when productive rate was identical with the catalyzer yield, total cellar for storing things of two reactors was less than the volume of single reactor.
Vapor phase process production is adopted in the crushing-resistant copolymerization reaction of Spheripol technology, and reactor is one or two placed in-line dense fluidized bed bioreactor.
Adopt a liquid-gas phase reactor system can produce the impact copolymer of ethylene content at 8%～12% (massfraction).It is higher and may have the special impact copolymer (as the low-stress product that turns white) of an above disperse phase to produce rubber phase content as need, then need to design two liquid-gas phase reactor systems, keep gas phase composition and operational condition in two liquid-gas phase reactor systems independent, can obtain two kinds of different multipolymers and add in the homopolymer.
The Borstar of Borealis (Borealis) (northern star is bimodal) polymarization method for prodcing polyacrylates is the novel polymarization method for prodcing polyacrylates that just began to develop in 1998.Adopting double-reactor is that annular-pipe reactor series connection Gas-phase reactor is produced homopolymer and random copolymers, one or two Gas-phase reactor of connecting are again produced impact copolymers, annular-pipe reactor is similar to the annular-pipe reactor of Spheripol technology, but design pressure is higher.Because the molecular weight distribution of the bimodal handicraft product of northern star can be regulated from being too narrow in the wide range very much at an easy rate, is well suited for using single site catalysts.
The utility model content
The purpose of this utility model with existing spheripol technology and borstar process modification and with they organically combine create a kind of novel, have flexibly, changeable, adapt to the polypropylene plant of characteristics such as marketability is strong.
Continuous homopolymerization of propylene described in the utility model or copolymerization device are made up of annular tube type pre-polymerization reactor, endless tube homopolymerization device, overcritical copolymerization reactor and endless tube copolymerization reactor; The propylene input tube, catalyzer configuration pipe, the triethyl aluminum input tube is connected by the input aperture of triethyl aluminum mixing tank with annular tube type pre-polymerization reactor middle part with the electron donor input tube, the delivery port that the annular tube type pre-polymerization reactor is positioned at the bottom is connected with the input aperture of endless tube homopolymerization device bottom, the delivery port that endless tube homopolymerization device is positioned at the middle part is connected with the input aperture at overcritical copolymerization reactor middle part, the delivery port of overcritical copolymerization reactor bottom is connected with the input aperture of endless tube copolymerization reactor bottom, the delivery port of endless tube copolymerization reactor bottom connects discharge nozzle, and overcritical copolymerization reactor bottom connects water cooler by pipeline, propylene compressor is communicated with overcritical copolymerization reactor top.
Technical process of the present utility model is as follows: purity 99.5% refining qualified propylene, with being pumped into the triethyl aluminum mixing that triethyl aluminum mixing tank and catalyzer arrangement unit are sent here, the water in the propylene is removed in reaction, oxygen, impurity such as carbon monoxide, the laggard annular tube type pre-polymerization reactor of sending here with the catalyzer arrangement unit of catalyst mix again, in the annular tube type pre-polymerization reactor, catalyzer and triethyl aluminum complexing form has active catalyzer, concurrent first portion polymerization. polypropylene, propylene and catalyzer enter endless tube homopolymerization device together, more than 4MP, carrying out homopolymerization under the condition of 70-80 degree. polypropylene and part propylene liquid enter overcritical copolymerization reactor together, the heat that the amount of liquid propene is taken away with vaporization is advisable than reaction heat is less slightly. and the outer gas-phase propene ethene that adds of the propylene of vaporization and reactor carries out copolyreaction, in homopolymer polypropylene,, add hydrogen and regulate melting index with outside growth second third glue.
Polypropylene that overcritical copolymerization reactor is come out and propylene liquid enter the endless tube copolymerization reactor together under the effect of initiate catalyzer, carry out copolyreaction with higher olefins such as initiate propylene, butene-1 or hexenes-1, the unreacted propylene of polypropylene and part goes the hypomere operation in the discharging of endless tube bottom together.
What carry out in the described endless tube homopolymerization device is homopolymerization, and reaction conditions is more than the 4MPa, 70～80 ℃.
Described polypropylene and the part propylene liquid that comes out from endless tube homopolymerization device enters overcritical copolymerization reactor together, and the heat that the amount of liquid propene is taken away with vaporization is advisable than reaction heat is less slightly.The outer gas-phase propene ethene that adds of the propylene of vaporization and reactor carries out copolyreaction, with outside growth second third glue, adds hydrogen and regulates melting index in homopolymer polypropylene.
Described overcritical copolymerization reactor can high temperature (85～95 ℃), high pressure (4～5MPa) or surpass under the condition of propylene critical temperature and/or emergent pressure and operate, can prevent the formation of bubble like this.
Described overcritical copolymerization reactor is operated under the dense bed condition, and ethene under gas phase or the super critical condition and propylene can arbitrary proportions, and the ratio of the ethylene-propylene rubber(EPR) in the polypropylene can be regulated arbitrarily.
Polypropylene and propylene liquid that described overcritical copolymerization reactor is come out enter the endless tube copolymerization reactor together, under the effect of initiate catalyzer, carry out copolyreaction with higher olefins such as initiate propylene, butene-1 or hexenes-1, the unreacted propylene of polypropylene and part goes the hypomere operation in the discharging of endless tube bottom together.
In the described endless tube copolymerization reactor liquid propene can and high-carbon a alkene arbitrary proportion such as hexene-1 dissolve each other, can increase the embedded quantity of higher olefins, improve the performance of product.Liquid propylene and hexene-1 can be washed fugitive constituent and the ash content in the product off simultaneously, improve the quality of product.
When the present invention produced alfon, then open loop pipe homopolymerization device and overcritical copolymerization reactor were utilized the difference of the phase of two reactor propylene, and the difference of temperature of reaction, pressure is produced high-quality bimodal homo-polypropylene.
During production second third copolymerized product of the present invention, then open loop pipe homopolymerization device and overcritical copolymerization reactor, endless tube homopolymerization device is produced homopolymer, and overcritical copolymerization reactor is produced ethylene-propylene rubber(EPR).
The present invention produces in the still alloy or introduces the 3rd copolymerization component, when particularly the 3rd copolymerization component of Yin Ruing is high-carbon a-alkene, and three reactor standard-sized sheet workers then.
The present invention has following characteristics:
First reaction mainly utilizes the homopolymerization of liquid phase annular-pipe reactor, and the many characteristics of product that polypropylene GRANULES is spherical in shape, particle is big, condition of high voltage can be produced are down operated second reactor under the dense bed condition.Second reactor adopts Gas-phase reactor, mainly is to utilize gas-phase reaction ethene and the propylene can arbitrary proportion the characteristics that the ratio of the ethylene-propylene rubber(EPR) in the polypropylene can be regulated arbitrarily.The 3rd reactor utilize in the liquid phase annular-pipe reactor liquid propene can and high-carbon a alkene arbitrary proportion such as hexene-1 dissolve each other, can increase the embedded quantity of higher olefins, improve the performance of product.Liquid propylene and hexene-1 can be washed fugitive constituent and the ash content in the product off simultaneously, improve the quality of product.
This process unit is flexible, changeable, if it is strong to adapt to marketability. produce alfon, then only open first, second reactor, utilize the difference of the phase of two reactor propylene, the difference of temperature of reaction, pressure is produced high-quality bimodal homo-polypropylene. production second third copolymerized product, first reactor is produced homopolymer, if second reactor is produced ethylene-propylene rubber(EPR). produce alloy in the still, or to introduce the 3rd copolymerization component that the 3rd copolymerization component particularly introduces be high-carbon a-alkene, then three reactor standard-sized sheet workers.
Description of drawings
Continuous homopolymerization of Fig. 1 propylene or copolymerization process device synoptic diagram.
Wherein: 1, triethyl aluminum input tube 2, catalyzer configuration pipe 3, propylene input tube 4, electron donor input tube 5, annular tube type pre-polymerization reactor 6, endless tube homopolymerization device 7, overcritical copolymerization reactor 8, propylene compressor 9, water cooler 10, endless tube copolymerization reactor 11, discharge nozzle
Embodiment
Continuous homopolymerization of propylene described in the utility model or copolymerization device are made up of annular tube type pre-polymerization reactor 5, endless tube homopolymerization device 6, overcritical copolymerization reactor 7 and endless tube copolymerization reactor 10; Propylene input tube 3, catalyzer configuration pipe 2, triethyl aluminum input tube 1 is connected by the input aperture of triethyl aluminum mixing tank with annular tube type pre-polymerization reactor 5 middle parts with electron donor input tube 4, the delivery port that annular tube type pre-polymerization reactor 5 is positioned at the bottom is connected with the input aperture of endless tube homopolymerization device 6 bottoms, the delivery port that endless tube homopolymerization device 6 is positioned at the middle part is connected with the input aperture at overcritical copolymerization reactor 7 middle parts, the delivery port of overcritical copolymerization reactor 7 bottoms is connected with the input aperture of endless tube copolymerization reactor 10 bottoms, the delivery port of endless tube copolymerization reactor 10 bottoms connects discharge nozzle 11, and overcritical copolymerization reactor 7 bottoms connect water cooler 9 by pipeline, propylene compressor 8 is communicated with overcritical copolymerization reactor 7 tops.
Claims (1)
1. continuous homopolymerization of propylene or copolymerization process device are made up of annular tube type pre-polymerization reactor, endless tube homopolymerization device, overcritical copolymerization reactor and endless tube copolymerization reactor; It is characterized in that: the propylene input tube, catalyzer configuration pipe, the triethyl aluminum input tube is connected by the input aperture of triethyl aluminum mixing tank with annular tube type pre-polymerization reactor middle part with the electron donor input tube, the delivery port that the annular tube type pre-polymerization reactor is positioned at the bottom is connected with the input aperture of endless tube homopolymerization device bottom, the delivery port that endless tube homopolymerization device is positioned at the middle part is connected with the input aperture at overcritical copolymerization reactor middle part, the delivery port of overcritical copolymerization reactor bottom is connected with the input aperture of endless tube copolymerization reactor bottom, the delivery port of endless tube copolymerization reactor bottom connects discharge nozzle, and overcritical copolymerization reactor bottom connects water cooler by pipeline, propylene compressor is communicated with overcritical copolymerization reactor top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009201107621U CN201459002U (en) | 2009-08-07 | 2009-08-07 | Continuous propylene homopolymerization or copolymerization process device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009201107621U CN201459002U (en) | 2009-08-07 | 2009-08-07 | Continuous propylene homopolymerization or copolymerization process device |
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| Publication Number | Publication Date |
|---|---|
| CN201459002U true CN201459002U (en) | 2010-05-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009201107621U Expired - Lifetime CN201459002U (en) | 2009-08-07 | 2009-08-07 | Continuous propylene homopolymerization or copolymerization process device |
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| CN (1) | CN201459002U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585352A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工股份有限公司 | Stress whitening-resistant and impact-resistant polypropylene composite |
-
2009
- 2009-08-07 CN CN2009201107621U patent/CN201459002U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585352A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工股份有限公司 | Stress whitening-resistant and impact-resistant polypropylene composite |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100512 |