CN114075309A - Method and system for regulating and controlling polyolefin performance - Google Patents
Method and system for regulating and controlling polyolefin performance Download PDFInfo
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- CN114075309A CN114075309A CN202010801584.8A CN202010801584A CN114075309A CN 114075309 A CN114075309 A CN 114075309A CN 202010801584 A CN202010801584 A CN 202010801584A CN 114075309 A CN114075309 A CN 114075309A
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
Abstract
The invention relates to a method and a system for regulating and controlling polyolefin performance. In the method, liquid materials obtained by compressing, condensing and gas-liquid separating unreacted circulating materials in a second reactor are conveyed back to a first reactor and the second reactor to form a cycle; meanwhile, the tail gas recovery system is utilized to compress and separate the effluent of the polymerization reaction system, and the obtained recovered feed liquid is returned to the first reactor and the second reactor again to form another cycle; the concentration and the temperature of reaction materials in the two reactors in a polymerization reaction system are regulated and controlled by regulating the flow proportion of the recovered feed liquid and/or the liquid material returned to the first reactor and the second reactor, so that the performance of polyolefin products in the two reactors is regulated and controlled, and the performance of final products is regulated and controlled. The method can regulate and control the performance of the polyolefin more flexibly and in a larger range, and has good economical efficiency.
Description
Technical Field
The invention belongs to the technical field of olefin polymerization, and particularly relates to a method and a system for regulating and controlling polyolefin performance.
Background
Unlike small molecules, polyolefins have the characteristics of a multilevel structure, which makes the regulation principle and means for polyolefin performance quite complex. The multilevel structure mainly comprises a molecular chain structure and an aggregation state structure, wherein the molecular chain structure comprises composition, molecular weight and distribution thereof, a branched chain sequence structure, isotacticity and the like; the aggregated structure includes chain entanglement, chain crystallization, chain orientation, and the like. How to regulate and control the directional arrangement of the multilevel structure and endow the polyolefin with the required performance is the key for realizing the high performance of the polyolefin product and meeting the market demand. The regulation and control of the molecular weight and the distribution, the branching degree distribution, the melt index, the density and other product properties can be carried out by the following variables: (1) reaction temperature, catalyst feed rate, comonomer feed rate, condensate feed position and flow, and catalyst type. The above are main control variables, which can directly influence the product performance. (2) Reactor pressure, circulating gas flow rate, bed level. This is a secondary control variable and is not a direct factor in the performance variables and should not be changed frequently. (3) Polymerization monomer feeding rate, polymerization monomer partial pressure, poison concentration, product discharge frequency and residence time. This is an intermediate variable, which is influenced by the primary control variable. The regulation of product properties is therefore usually focused on changes in the main control variables.
In patent CN106928383B, a plurality of liquid material inlets are arranged on the side wall of a reactor, so that the environmental temperature in the reactor is controlled at a plurality of positions, and the branching degree of a product is improved; patent CN104628904B utilizes a circulating medium to form multiple polymerization reaction zones with different temperatures from top to bottom in a fluidized bed reactor, thereby realizing the preparation of high performance polyolefin products in a single reactor; patent CN201510674100.7 uses a dual reactor end-to-end reaction system to produce polyolefins. However, these methods have a limited range of adjustment of the composition of the monomer and the condensate in the fluidized bed, the performance adjustment is limited, and the recovered liquid is not utilized properly.
It is therefore desirable to provide a new process that allows a greater range of tailoring of polyolefin properties.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method for regulating and controlling the performance of polyolefin, which utilizes a tail gas recovery system to compress and separate the outflow material of a polymerization reaction system to obtain recovered feed liquid; in addition, discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials after compression, condensation and gas-liquid separation; the concentration and the temperature of reaction materials in the two reactors in a polymerization reaction system are regulated and controlled by regulating the flow proportion of the recovered feed liquid and/or the liquid material returned to the first reactor and the second reactor, so that the performance of polyolefin products in the two reactors is regulated and controlled, and the performance of final products is regulated and controlled. The method can regulate and control the performance of the polyolefin more flexibly and in a larger range, and simultaneously, the recovered feed liquid recovered by the tail gas recovery system is fully utilized.
To this end, the present invention provides in a first aspect a method for tailoring properties of a polyolefin comprising the steps of:
s1, introducing olefin monomer, catalyst and molecular weight regulator into a polymerization reaction system comprising a first reactor and a second reactor;
s2, the olefin monomer and the catalyst are pre-polymerized after contacting in the first reactor to generate first polyolefin;
s3, allowing the material containing the first polyolefin to enter a second reactor for further polymerization reaction to generate polyolefin;
s4, discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; the liquid material is conveyed back to the first reactor and the second reactor, and the first gas material is conveyed back to the second reactor;
s5, discharging the mixed material containing the polyolefin from the bottom of the second reactor, and degassing by a degassing bin to obtain polyolefin and a second gas material;
s6, introducing the second gas material to a tail gas recovery system, compressing and separating to obtain a recovered material liquid, and introducing the recovered material liquid back to the first reactor and the second reactor;
and controlling the performance of the polyolefin by controlling the ratio of the recovered feed liquid to the first reactor and the second reactor and/or the ratio of the liquid material to the first reactor and the second reactor.
In the present invention, the mixture containing the polyolefin may be continuously discharged from the bottom of the second reactor or intermittently discharged from the bottom of the second reactor.
In some preferred embodiments of the present invention, the recycle feed stream is fed to the first reactor and the second reactor at a ratio of (0-1): 0-1. According to the invention, by flexibly controlling the ratio of the recovered material liquid to the first reactor and the second reactor, on one hand, the flow composition of streams input into the two reactors can be changed under the condition that the flow of the streams input into the reactors is not changed, and on the other hand, the flow of the streams input into the two reactors can be changed, so that the performance of polyolefin can be flexibly regulated and controlled in a wider range; meanwhile, the recovered feed liquid is fully utilized.
In other preferred embodiments of the present invention, the ratio of the liquid feed stream to the first reactor to the second reactor stream is (0-1): (0-1). Similarly, by flexibly controlling the flow ratio of the liquid material to be input into the first reactor and the second reactor, on one hand, the flow composition of the streams input into the two reactors can be changed under the condition that the flow rate of the streams input into the reactors is not changed, on the other hand, the flow rate of the streams input into the two reactors can be changed, and further, the performance of the polyolefin can be flexibly regulated and controlled in a wider range.
In some embodiments of the invention, the unreacted recycled material in the second reactor comprises at least one olefin monomer; it is preferable to further include at least two of a cocatalyst, a molecular weight regulator and an inert gas.
In other embodiments of the present invention, the first gaseous feed and/or the second gaseous feed comprises at least one olefin monomer; it is preferable to further include at least two of a cocatalyst, a molecular weight regulator and an inert gas.
It is to be noted that, when the gas-liquid separation in step S4 is incomplete, the first gaseous material at this time may contain a part of the liquid material.
In the present invention, the olefin monomer, the catalyst and the molecular weight regulator introduced into the polymerization reaction system may be introduced before the start of the reaction, or may be introduced during the reaction. The location of introduction is also not limited to the inlets of the first and second reactors, but may also be introduced in a gas transfer line, such as a transfer line for discharging unreacted recycled material from the second reactor. Meanwhile, in addition to the olefin monomer, the catalyst and the molecular weight modifier, a co-catalyst, an inert gas, etc. may be introduced into the polymerization reaction system.
In some embodiments of the invention, the olefin monomer is selected from at least one of ethylene and an alpha-olefin having less than 18 carbon atoms. In some embodiments of the invention, the alpha-olefin is selected from at least one of alpha-olefins of 4 to 18 carbon atoms; preferably, the alpha-olefin is selected from at least one of butene, hexene and octene.
In some embodiments of the invention, the catalyst introduced in the first and second reactors is each independently selected from one or more of a chromium-based catalyst, a ziegler-natta catalyst (Z-N catalyst), a metallocene catalyst, and a late transition metal catalyst. In the present invention, the catalyst introduced into the first reactor and the second reactor may be the same catalyst or different catalysts.
In other embodiments of the present invention, the reaction pressure of the first reactor is 1.0 to 10MPa, and the reaction temperature is 40 to 100 ℃; the reaction pressure of the second reactor is 0.5-9.5 MPa, and the reaction temperature is 60-120 ℃. The reaction temperature and reaction pressure in the first reactor and the second reactor can cooperate with the ratio of the recovered feed liquid to the first reactor and the second reactor stream and/or the ratio of the liquid material to the first reactor and the second reactor stream to regulate the properties of the polyolefin.
In some embodiments of the invention, the recovered feed liquid obtained in step S6 has a different composition than at least one of the liquid feed obtained in step S4 and the feed comprising the first polyolefin entering the second reactor in step S3. Specifically, the recovered feed liquid obtained in step S6 is different in composition of the liquid phase from at least one of the liquid material obtained in step S4 and the material including the first polyolefin entering the second reactor in step S3. Therefore, after the two materials (the recycled material liquid and the liquid material) with different proportions are introduced into the reactor, the material composition in the reactor is influenced, so that the proportion regulation of the olefin monomer and the molecular weight regulator in the liquid phase, the gas phase and the solid phase is more flexible, the reaction environment in the reactor is regulated, and the performance of the polyolefin is further changed.
In some embodiments of the invention, the properties of the polyolefin include, but are not limited to, one or more of the polyolefin's molecular weight and its distribution, branching degree distribution, melt index, and density.
The invention provides a system for regulating and controlling the performance of polyolefin, which comprises a polymerization reaction system, a degassing bin and a tail gas recovery system which are connected end to end in sequence; wherein the polymerization reaction system comprises a first reactor and a second reactor which are connected end to end.
In some embodiments of the invention, the tail gas recovery system comprises an end-to-end compression system and a separation system.
In some preferred embodiments of the invention, the separation system comprises an end-to-end oligomer removal system and a dual expansion self-cryogenic separation system.
The process of the present invention uses a homo-and copolymerization system using olefins as the reaction raw material. The terms "homopolymerization" and "copolymerization" as used herein mean that the polymerization system comprises one polymerizable monomer and at least two polymerizable monomers, respectively.
The invention has the beneficial effects that: according to the method, the liquid material obtained by compressing, condensing and gas-liquid separating the unreacted circulating material in the second reactor is conveyed back to the first reactor and the second reactor to form a cycle, and meanwhile, a tail gas recovery system and a polymerization reaction system form another cycle outside the polymerization reaction system, so that the feeding number of the first reactor and the second reactor is increased, the adjustment of the polymerization reaction environment of the two reactors is more flexible, and the performance of the polyolefin can be adjusted and controlled in a larger range. Meanwhile, the composition of the recovered feed liquid obtained after the materials flowing out of the polymerization reaction system are separated and purified by the tail gas recovery system is changed, and the recovered feed liquid is conveyed back to the polymerization reaction system to regulate and control the polymerization environment, so that the economy is good.
Drawings
The invention will be further explained with reference to the drawings.
FIG. 1 is a schematic flow diagram of a system for tailoring polyolefin properties according to one embodiment of the present invention; wherein the reference numerals in the figures have the meaning:
1 a first reactor for the prepolymerization of olefins;
2 a heat exchanger for removing heat from the first reactor;
3 a distribution plate for uniformly distributing gas at the bottom of the fluidized bed reactor (second reactor);
4 a second reactor for the polymerization of olefins;
5 a recycle gas compressor for maintaining a recycle gas stream flowing in the conduit;
6 a heat exchanger for cooling the circulating gas stream;
7 a device for gas-liquid separation;
a storage tank 8 for storing the liquid separated by the gas-liquid separation device 7;
9 a pump for pumping the liquid material into the first reactor and the second reactor;
10 degassing chamber for degassing polyolefins;
11 a compressor for boosting the pressure of the gaseous material;
12 a cooler for cooling the high pressure gas material;
13 means for removing oligomers;
14 equipment for self heat exchange of the cryogenic system;
15 means for gas-liquid separation;
16 apparatus for gas expansion refrigeration;
17 valves for throttling refrigeration;
18 a pump for delivering the separated liquid back to the polymerization system;
19 a recycle conduit for redistributing gas in the second reactor within the vessel;
20 a conduit for introducing polymerized monomer;
21 a conduit for introducing a molecular weight regulator;
22 a conduit for introducing a catalyst into the second reactor;
23 a conduit for withdrawing a mixture comprising polyolefin product from the second reactor and introducing into the degassing silo;
24 a conduit for returning the liquid material stored in the tank 8 to the first reactor;
25 a conduit for feeding the first polyolefin produced in the first reactor to the second reactor;
26 a conduit for introducing polymerized monomer into the first reactor;
27 a conduit for introducing a molecular weight regulator into the first reactor;
28 a conduit for introducing catalyst into the first reactor;
29 a conduit for introducing the cocatalyst into the second reactor;
30 a conduit for returning the liquid material stored in the storage tank 8 to the second reactor;
31 a pipeline for feeding the material treated by the compression system into the cryogenic system;
32 a circulating pipeline for conveying the material treated by the compression system back to the polymerization reaction system;
33, a pipeline for inputting the separated gas treated by the cryogenic system into an available system;
34 is used for inputting the separated gas treated by the cryogenic system into a pipeline of an available system;
35 is used for inputting the materials processed by the cryogenic system into a pipeline of an available system;
36 a pipeline for returning the recovered feed liquid obtained by the tail gas recovery system to the second reactor;
37 a pipeline for returning the recovered feed liquid obtained by the tail gas recovery system to the first reactor;
38 for the output of polyolefin products.
In a preferred embodiment, the polymerization system is connected end-to-end with the tail gas recovery system via the material transfer device 18 and the lines 32, 36 and 37. Wherein the sum of the materials in line 32 (i.e., the recycled feed liquid is comprised of the material processed by the compression system and the material processed by the cryogenic system) is equal to the sum of the materials in lines 36 and 37, the material compositions in lines 36 and 37 are the same, and there may be at most two flow rates of 0. The difference in the flow distribution of the lines 36 and 37 from at least one of the composition of the material output from the separator 7 and the composition of the material output from the line 25 results in a different ratio of the material output from the separator 7, thereby changing the polymerization conditions in the first and second reactors for the purpose of adjusting the properties of the polyolefin.
FIG. 2 is the material composition information of each stream when the ratio of the recovered feed liquid input into the second reactor to the first reactor stream is 1:0 in the present invention. The comonomer is 1-butene, the polymerization monomer is ethylene, and the molecular weight regulator is hydrogen. In fig. 2, the abscissa is the name of each stream, the recovered feed liquid is the output stream of the tail gas recovery system, and the ordinate is the molar ratio of the comonomer to the polymerized monomer, and the molecular weight regulator to the polymerized monomer. The ratio of the comonomer polymerization monomer in the recovered feed liquid is higher than that of the materials at the inlets of the first reactor and the second reactor, and the ratio of the molecular weight regulator to the polymerization monomer is lower than that of the materials at the inlets of the first reactor and the second reactor.
FIG. 3 is a graph of different feed compositions versus product density for a first reactor in accordance with one embodiment of the present invention. The comonomer is hexene and the polymeric monomer is ethylene. The abscissa is the hexene to ethylene molar ratio in the first reactor and the ordinate is the density value of the polyolefin product output from the second reactor. As can be seen from FIG. 3, the density of the polyolefin product decreases with increasing hexene to ethylene molar ratio, and the relationship curve shows a non-linear negative correlation. Therefore, the polymerization environment in the first reactor and the second reactor can be regulated and controlled by regulating and controlling the ratio of the recovered feed liquid to the flow of the first reactor and the second reactor, and the performance of the polyolefin can be regulated and controlled.
Detailed Description
In order that the present invention may be more readily understood, the following detailed description will proceed with reference being made to examples, which are intended to be illustrative only and are not intended to limit the scope of the invention. The starting materials or components used in the present invention may be commercially or conventionally prepared unless otherwise specified.
Example 1:
the Low Density Polyethylene (LDPE) is produced in a regulation and control system shown in figure 1, a first reactor 1 is used for carrying out binary copolymerization prepolymerization on ethylene and 1-butylene in the presence of a Z-N catalyst system at a polymerization temperature of 60 ℃, a polymerization pressure of 4.0MPa and a slurry mass fraction of 40%, and a stream containing the first polyolefin generated after prepolymerization is recycled to a second reactor by pressure for further polymerization. The second reactor is in an environment with a Z-N catalyst system, the polymerization temperature is 88 ℃, the polymerization pressure is 2.3MPa, the ethylene partial pressure is 0.8MPa, and the fluidizing gas velocity is 0.7m/s, the mixed material containing the polyolefin generated by polymerization enters a tail gas recovery system for compression and separation after being degassed by a degassing bin, the obtained recovered feed liquid is introduced back to the first reactor and the second reactor, and the mass ratio of the flow rates of the pipelines 36 and 37 is 1: 0.15. Discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; the liquid material is fed back to the first and second reactors and the first gas material is fed back to the second reactor, the mass ratio of the flow rates of the lines 30 and 24 being 1: 0.72.
The polyethylene produced according to example 1 had a melt index of 24.60g/10min and a density of 0.954g/cm3。
Example 2:
the Low Density Polyethylene (LDPE) is produced in a regulation and control system shown in figure 1, a first reactor 1 is used for carrying out binary copolymerization prepolymerization on ethylene and hexene in an environment with a Z-N catalyst system, wherein the polymerization temperature is 60 ℃, the polymerization pressure is 4.0MPa, the mass fraction of slurry is 40%, and a stream containing the first polyolefin generated after prepolymerization is recycled to a second reactor by pressure for further polymerization. The second reactor is in an environment with a Z-N catalyst system, the polymerization temperature is 88 ℃, the polymerization pressure is 2.3MPa, the ethylene partial pressure is 0.8MPa, and the fluidizing gas velocity is 0.7m/s, the mixed material containing polyolefin generated by polymerization enters a tail gas recovery system for compression and separation after being degassed by a degassing bin, the obtained recovered feed liquid is introduced back to the first reactor and the second reactor, and the mass ratio of the flow rates of the pipelines 36 and 37 is 1:0. Discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; returning the liquid material to the first and second reactors and the first gas material to the second reactor, the mass ratio of the flow rates of the streams 30 and 24 being 0.77:1
The polyethylene produced according to example 2 had a melt index of 27.24g/10min and a density of 0.954g/cm3。
Example 3:
the Low Density Polyethylene (LDPE) is produced in a regulation and control system shown in figure 1, a first reactor 1 is used for carrying out binary copolymerization prepolymerization on ethylene and 1-butylene in an environment with a Z-N catalyst system, the polymerization temperature is 60 ℃, the polymerization pressure is 4.0MPa, the mass fraction of slurry is 50%, and a stream containing the first polyolefin generated after prepolymerization is recycled to a second reactor by pressure for further polymerization. The second reactor is in an environment with a Z-N catalyst system, the polymerization reaction temperature is 88 ℃, the polymerization pressure is 2.3MPa, the ethylene partial pressure is 0.8MPa, and the fluidizing gas velocity is 0.7m/s, the mixed material containing polyolefin generated by polymerization enters a tail gas recovery system for compression and separation after being degassed by a degassing bin, the obtained recovered feed liquid is led back, and the mass ratio of the flow rates of the pipelines 36 and 37 is 1:0. Discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; the liquid material is fed back to the first and second reactors and the first gas material is fed back to the second reactor, the mass ratio of the flow rates of the lines 30 and 24 being 1: 0.64.
The polyethylene produced according to example 3 had a melt index of 36.29g/10min and a density of 0.955g/cm3。
Example 4:
the Low Density Polyethylene (LDPE) is produced in a regulation and control system shown in figure 1, a first reactor 1 is used for carrying out binary copolymerization prepolymerization on ethylene and hexene in an environment with a Z-N catalyst system, wherein the polymerization temperature is 60 ℃, the polymerization pressure is 4.0MPa, the mass fraction of slurry is 30%, and a stream containing the first polyolefin generated after prepolymerization is recycled to a second reactor by pressure for further polymerization. The second reactor is in an environment with a Z-N catalyst system, the polymerization reaction temperature is 88 ℃, the polymerization pressure is 2.3MPa, the ethylene partial pressure is 0.8MPa, and the fluidizing gas velocity is 0.7m/s, the mixed material containing polyolefin generated by polymerization enters a tail gas recovery system for compression and separation after being degassed by a degassing bin, the obtained recovered feed liquid is introduced back to the polymerization reaction system, and the mass ratio of the flow rates of the pipelines 36 and 37 is 1:0. Discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; the liquid material is fed back to the first and second reactors and the first gas material is fed back to the second reactor, the mass ratio of the flow rates of the lines 30 and 24 being 0.17: 1.
The polyethylene produced according to example 4 had a melt index of 24.09g/10min and a density of 0.953g/cm3。
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (10)
1. A method of tailoring properties of a polyolefin comprising the steps of:
s1, introducing olefin monomer, catalyst and molecular weight regulator into a polymerization reaction system comprising a first reactor and a second reactor;
s2, the olefin monomer and the catalyst are pre-polymerized after contacting in the first reactor to generate first polyolefin;
s3, allowing the material containing the first polyolefin to enter a second reactor for further polymerization reaction to generate polyolefin;
s4, discharging unreacted circulating materials in the second reactor from the top, and obtaining liquid materials and first gas materials after compression, condensation and gas-liquid separation; the liquid material is conveyed back to the first reactor and the second reactor, and the first gas material is conveyed back to the second reactor;
s5, discharging the mixed material containing the polyolefin from the bottom of the second reactor, and degassing by a degassing bin to obtain polyolefin and a second gas material;
s6, introducing the second gas material to a tail gas recovery system, compressing and separating to obtain a recovered material liquid, and introducing the recovered material liquid back to the first reactor and the second reactor;
and controlling the performance of the polyolefin by controlling the ratio of the recovered feed liquid to the first reactor to the second reactor and/or the ratio of the liquid material to the first reactor to the second reactor.
2. The method of claim 1, wherein the recycle feed is fed to the first reactor and the second reactor stream in a ratio of (0-1): 0-1; and/or
The ratio of the liquid material to the first reactor to the second reactor is (0-1) to (0-1).
3. The process of claim 1 or 2, wherein the unreacted recycled material in the second reactor comprises at least one olefin monomer; it is preferable to further include at least two of a cocatalyst, a molecular weight regulator and an inert gas.
4. The method of any one of claims 1-3, wherein the first gaseous feed and/or the second gaseous feed comprises at least one olefin monomer; it is preferable to further include at least two of a cocatalyst, a molecular weight regulator and an inert gas.
5. The method of claim 3 or 4, wherein the olefin monomer is selected from at least one of ethylene and an alpha-olefin having less than 18 carbon atoms.
6. The process of any of claims 1-5, wherein the catalyst introduced in the first reactor and the second reactor is each independently selected from one or more of a chromium-based catalyst, a Ziegler-Natta catalyst, a metallocene catalyst, and a late transition metal catalyst.
7. The method according to any one of claims 1 to 6, wherein the reaction pressure of the first reactor is 1.0 to 10MPa, and the reaction temperature is 40 to 100 ℃; the reaction pressure of the second reactor is 0.5-9.5 MPa, and the reaction temperature is 60-120 ℃.
8. The method according to any one of claims 1 to 7, wherein the recycled liquor obtained in step S6 has a different composition from at least one of the liquid feed obtained in step S4 and the feed comprising the first polyolefin entering the second reactor in step S3.
9. A system for regulating and controlling polyolefin performance comprises a polymerization reaction system, a degassing bin and a tail gas recovery system which are sequentially connected end to end; wherein the polymerization reaction system comprises a first reactor and a second reactor which are connected end to end.
10. The system of claim 9, wherein the tail gas recovery system comprises an end-to-end compression system and a separation system; preferably, the separation system comprises an end-to-end oligomer removal system and a dual expansion self-cryogenic separation system.
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| CN114957530A (en) * | 2022-06-28 | 2022-08-30 | 杭州双安科技有限公司 | Solution polymerization method of ethylene and alpha-olefin |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105199031A (en) * | 2015-10-16 | 2015-12-30 | 浙江大学 | Olefin polymerization method and device |
| CN106749819A (en) * | 2016-11-25 | 2017-05-31 | 联泓新材料有限公司 | A kind of production method of impact copolymer polypropylene |
| CN109682166A (en) * | 2018-12-03 | 2019-04-26 | 浙江大学 | A kind of emission recovery system that gas wave refrigeration is used for olefin polymetiation process |
-
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105199031A (en) * | 2015-10-16 | 2015-12-30 | 浙江大学 | Olefin polymerization method and device |
| CN106749819A (en) * | 2016-11-25 | 2017-05-31 | 联泓新材料有限公司 | A kind of production method of impact copolymer polypropylene |
| CN109682166A (en) * | 2018-12-03 | 2019-04-26 | 浙江大学 | A kind of emission recovery system that gas wave refrigeration is used for olefin polymetiation process |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114957530A (en) * | 2022-06-28 | 2022-08-30 | 杭州双安科技有限公司 | Solution polymerization method of ethylene and alpha-olefin |
| CN114957530B (en) * | 2022-06-28 | 2023-09-29 | 杭州双安科技有限公司 | Solution polymerization method of ethylene and alpha-olefin |
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