CN117924570A - Polyolefin production device and method with strong robustness - Google Patents
Polyolefin production device and method with strong robustness Download PDFInfo
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- CN117924570A CN117924570A CN202211314175.0A CN202211314175A CN117924570A CN 117924570 A CN117924570 A CN 117924570A CN 202211314175 A CN202211314175 A CN 202211314175A CN 117924570 A CN117924570 A CN 117924570A
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 69
- 229920000098 polyolefin Polymers 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 239000004711 α-olefin Substances 0.000 claims abstract description 38
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000000178 monomer Substances 0.000 claims description 38
- 239000003054 catalyst Substances 0.000 claims description 33
- 238000002156 mixing Methods 0.000 claims description 23
- 239000000047 product Substances 0.000 claims description 23
- 238000010992 reflux Methods 0.000 claims description 17
- 239000003607 modifier Substances 0.000 claims description 16
- 239000007795 chemical reaction product Substances 0.000 claims description 14
- 239000000463 material Substances 0.000 claims description 9
- 230000035484 reaction time Effects 0.000 claims description 9
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims description 8
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 239000002904 solvent Substances 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 5
- -1 ethylene, propylene, 1-butene Chemical class 0.000 claims description 5
- TVMXDCGIABBOFY-UHFFFAOYSA-N n-Octanol Natural products CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 4
- 229920000642 polymer Polymers 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000012190 activator Substances 0.000 claims description 2
- 239000002216 antistatic agent Substances 0.000 claims description 2
- 239000012018 catalyst precursor Substances 0.000 claims description 2
- 239000012986 chain transfer agent Substances 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 239000011261 inert gas Substances 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 238000006116 polymerization reaction Methods 0.000 abstract description 10
- 239000000203 mixture Substances 0.000 description 9
- 239000003426 co-catalyst Substances 0.000 description 8
- 150000001336 alkenes Chemical class 0.000 description 7
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 7
- 238000012546 transfer Methods 0.000 description 6
- 239000003153 chemical reaction reagent Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000011265 semifinished product Substances 0.000 description 4
- 238000007334 copolymerization reaction Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 229920001577 copolymer Polymers 0.000 description 2
- 229920001971 elastomer Polymers 0.000 description 2
- 239000000806 elastomer Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 229920006124 polyolefin elastomer Polymers 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229920001400 block copolymer Polymers 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000012840 feeding operation Methods 0.000 description 1
- 229920001903 high density polyethylene Polymers 0.000 description 1
- 239000004700 high-density polyethylene Substances 0.000 description 1
- 229920001519 homopolymer Polymers 0.000 description 1
- 229920001684 low density polyethylene Polymers 0.000 description 1
- 239000004702 low-density polyethylene Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 229920005604 random copolymer Polymers 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
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- Polymerisation Methods In General (AREA)
Abstract
The invention relates to the technical field of polyolefin production, and provides a polyolefin production device and method with strong robustness. The polyolefin production device and the polyolefin production method provided by the invention have flexible operation modes, are convenient for switching different process conditions according to raw materials and products, can adapt to different alpha-olefin polymerization reaction conditions, and realize continuous, intermittent or semi-continuous operation; meanwhile, the reaction temperature can be accurately controlled, the safety and the reliability of the production process are improved, and various polyolefin products including high-end polyolefin products can be produced on the same set of device through a switching process.
Description
Technical Field
The invention relates to the technical field of polyolefin production, in particular to a polyolefin production device and a polyolefin production method with strong robustness.
Background
In the plastic consumption, the polyolefin accounts for more than 60 percent, and is the plastic variety with the largest consumption. Polyolefin products include some conventional polymeric materials such as low density polyethylene, high density polyethylene, linear low density ethylene, polypropylene, and the like. With the continuous progress of technology, polyolefin products are being developed to high-end fields such as poly-1-butene, ethylene-propylene-diene copolymer, ethylene/alpha-olefin random copolymer elastomer, block copolymer elastomer, and the like. Currently, in order to improve the competitiveness of products, domestic polyolefin production enterprises are increasing technological investment and reducing production cost; meanwhile, the product marks are increased, and the flexibility and the diversity of the production device are improved, so that the polyolefin product has a place in the high-end market.
However, since polyolefin products are various in variety and different in production conditions, enterprises are difficult to make reasonable trade-off comparison between the product variety and investment cost, and international situations are changeable, if the product production technology cannot be quickly and flexibly adapted to market changes, economic benefits of the enterprises are seriously affected.
Chinese patent CN102190742a discloses an olefin polymerization apparatus and an olefin polymerization method, the apparatus includes a reactor, a circulating gas heat exchanger, a gas-liquid separation tank, and a device for removing powder and mist, but the variety of products which can be produced by switching is very limited due to the simple function of the reaction part. Chinese patent CN105732849a discloses an olefin polymerization apparatus and method, the apparatus includes a polymerization reactor, a gas-liquid separator, a storage tank, etc., which can realize copolymerization and homo-polymerization of olefin, and switching between copolymerization and copolymerization, but the production process lacks flexibility and stability, and limits the performance of polyolefin products.
Therefore, it is of great importance to develop olefin polymerization plants and processes which can be adapted to different reaction conditions and which can be switched to produce a variety of polyolefin products.
Disclosure of Invention
The invention aims to provide a polyolefin production device and a polyolefin production method with strong robustness, so as to solve the technical problem that the olefin polymerization device and the olefin polymerization method in the prior art cannot be well switched to produce various polyolefin products.
In order to achieve the above purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a polyolefin production apparatus with strong robustness, comprising a prepolymerization reactor, a main reactor set, a hybrid refiner and a buffer tank;
The raw material feeding pipe is divided into two branches, wherein one branch is connected with the main reactor group through a second control valve and is connected with the mixing refiner through a first control valve; the other branch is connected with a main catalyst feeding pipe and an auxiliary catalyst feeding pipe, and the other branch is connected with a prepolymerization reactor which is connected with a main reactor group;
The discharging channel of the main reactor group is divided into two branches, wherein one branch is connected to the device boundary region through a sixth control valve; the other branch is connected with the mixing refiner through a third control valve; the mixing refiner is also connected with a refiner feed pipe; the discharging channel of the mixing refiner is connected with the buffer tank;
The discharging channel of the buffer tank is divided into two branches, one branch is connected to the device boundary region through a fourth control valve, and the other branch is connected with the main reactor group through a fifth control valve;
The main reactor group is provided with a temperature control loop.
As a preferred embodiment of the polyolefin production apparatus provided by the present invention, the main reactor group comprises at least two main reactors;
Preferably, the main reactors are connected in series or parallel; and/or the main reactor is a stirred tank reactor or a loop reactor.
As another preferred embodiment of the polyolefin production apparatus provided by the present invention, further comprising a top cooling device connected to the main reactor group; preferably, the top cooling device comprises a top cooler and a top reflux drum;
and/or the main reactor group is connected with a modifier feeding pipe (004).
In a second aspect, the present invention provides a method for producing a polyolefin with strong robustness, applied to the above-mentioned polyolefin production apparatus, wherein the polyolefin production method can switch between two production modes, namely, production mode i and production mode ii, according to the raw materials and product schemes:
Production mode i includes:
The first alpha-olefin monomer in the raw material feeding pipe is split into two streams, wherein one stream of the first alpha-olefin monomer is conveyed to a prepolymerization reactor to be mixed together with a main catalyst in a main catalyst feeding pipe and an auxiliary catalyst in an auxiliary catalyst feeding pipe, and the mixed stream is conveyed to a main reactor group;
The other one of the first alpha-olefin monomers is conveyed to a mixing refiner, and the optional second alpha-olefin monomer or solvent is conveyed to the mixing refiner through a feeding pipe of the refiner, and the material flow output by the mixing refiner is conveyed to a buffer tank and then conveyed to a main reactor group by the buffer tank;
after the reaction in the main reactor group is finished, the reaction product is discharged and conveyed to a device boundary region;
Production mode ii includes:
The first alpha-olefin monomer in the raw material feeding pipe is split into two streams, wherein one stream of the first alpha-olefin monomer is conveyed to a prepolymerization reactor to be mixed together with a main catalyst in a main catalyst feeding pipe and an auxiliary catalyst in an auxiliary catalyst feeding pipe, and the mixed stream is conveyed to a main reactor group;
another stream of the first alpha-olefin monomer is directly fed to the main reactor set;
After the reaction in the main reactor set is finished, the reaction product is conveyed to a mixing refiner, meanwhile, the optional second alpha-olefin monomer, solvent or modifier is also conveyed to the mixing refiner through a refiner feed pipe, the material flow output by the mixing refiner is conveyed to a buffer tank, after settling separation, part of the product is conveyed to a device boundary region, and the other part of solvent, unreacted monomer or unreacted complete polymer is conveyed back to the main reactor set.
As a preferred embodiment of the polyolefin production process provided by the present invention, production mode I further comprises: the modifier is directly conveyed to the main reactor group through a modifier feeding pipe.
As a preferred embodiment of the polyolefin production process provided by the present invention, production mode ii further comprises: the modifier is directly conveyed to the main reactor group through a modifier feeding pipe.
As a preferred embodiment of the polyolefin production process provided by the present invention, the main reactor train is temperature controlled by passing a utility stream into the temperature control loop.
As another preferred embodiment of the polyolefin production process provided by the present invention, the gas phase stream in the main reactor train is fed to an overhead cooler for cooling and then to an overhead reflux drum and back to the main reactor train.
As another preferable scheme of the polyolefin production method provided by the invention, the operation mode of the main reactor group is any one of continuous operation, batch operation and semi-continuous operation, and the operation period is any one of linearity, step and waveform.
As another preferable scheme of the polyolefin production method provided by the invention, the reaction temperature of the prepolymerization reactor is 30-100 ℃, the operation pressure is 0.5-4.5 MPa, and the reaction time is 1-60 min;
And/or the reaction temperature of the main reactor group is 50-150 ℃, the operation pressure is 0.5-4.5 MPa, the reaction time is 30-240 min, the operation liquid level is 50-90%, and the stirring speed is 30-150 r/min;
and/or the operating temperature of the top cooler is 20-60 ℃ and the operating pressure is 0.5-4.5 MPa;
and/or the operating temperature of the top reflux tank is 20-60 ℃ and the operating pressure is 0.5-4.5 MPa;
And/or the operation temperature of the mixing refiner is 20-150 ℃ and the operation pressure is 0.5-4 MPa;
And/or the operation temperature of the buffer tank is 30-200 ℃, the operation pressure is 0.5-4 MPa, and the residence time is 5-100 min.
As another preferred embodiment of the polyolefin production process provided by the present invention, the first alpha-olefin monomer comprises at least one of ethylene, propylene, 1-butene, 1-hexene and 1-octene.
As another preferable mode of the polyolefin production process provided by the invention, the second alpha-olefin monomer comprises at least one of ethylene, propylene, 1-butene, 1-hexene and 1-octene.
As another preferred embodiment of the polyolefin production process provided by the present invention, the procatalyst comprises at least one catalyst precursor, at least one activator and optionally at least one catalyst support;
and/or the modifier comprises at least one of antistatic agent, chain transfer agent, condensing agent and inert gas.
The invention has the advantages that:
The invention provides a polyolefin production device and a method with strong robustness, which have flexible operation modes, are convenient for switching different process conditions according to raw materials and products, can adapt to different alpha-olefin polymerization reaction conditions, and realize continuous, intermittent or semi-continuous operation; meanwhile, the reaction temperature can be accurately controlled, the safety and the reliability of the production process are improved, and various polyolefin products including high-end polyolefin products can be produced on the same set of device through a switching process.
Drawings
FIG. 1 is a schematic diagram of a polyolefin production apparatus with high robustness according to the present invention.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to specific embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the present invention in any way.
Unless defined otherwise, technical terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which the present invention pertains. The reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the raw materials, instruments, equipment, etc. used in the following examples are all commercially available or available by existing methods; the reagent dosage is the reagent dosage in the conventional experimental operation if no special description exists; the experimental methods are conventional methods unless otherwise specified.
The polyolefin production apparatus with strong robustness according to the present invention, as shown in fig. 1, comprises a prepolymerization reactor 102, a main reactor train, a mixing refiner 112 and a buffer tank 113.
The main reactor set comprises two main reactors 104/105; the two main reactors 104/105 are connected in series or in parallel by a seventh control valve 7 and an eighth control valve 8. Both main reactors 104/105 are connected to a top cooling device comprising a top cooler 106/109 and a top reflux drum 107/110. The top cooling device can obviously improve the heat removal capacity in the reaction process and effectively control the reaction intensity.
The raw material feeding pipe 001 is divided into two branches, wherein one branch is connected with the main reactor group through a second control valve 2 and is connected with the mixing refiner 112 through a first control valve 1; the other branch is connected with a main catalyst feeding pipe 002 and an auxiliary catalyst feeding pipe 003, and the other branch is connected with a prepolymerization reactor 102, and the prepolymerization reactor 102 is connected with a main reactor group.
The discharge channel of the main reactor group is divided into two branches, wherein one branch is connected to the device boundary region through a sixth control valve 6; the other branch is connected with the mixing refiner 112 through a third control valve 3; the mixer refiner 112 is also connected with a refiner feed pipe 007; the discharge passage of the mixing refiner 112 is connected to a buffer tank 113.
The discharge channel of the buffer vessel 113 is divided into two branches, one of which is connected to the plant area via a fourth control valve 4 and the other is connected to the main reactor group via a fifth control valve 5.
A temperature control loop 017 is provided on the main reactor set.
The main reactor group is also connected with a modifier feeding pipe 004.
The buffer tank 113 provided in the polyolefin production apparatus of the present invention has different functions in different production modes. When the reaction system is in the production mode I, different operation modes of the reaction process can be realized by changing the feeding operation period of the buffer tank 113; when the reaction system is in production mode II, recycling of the solvent, monomer or unreacted polymer can be achieved by heating the buffer tank 113.
Referring to the polyolefin production apparatus shown in fig. 1, different polyolefin products can be prepared by adjusting raw materials and switching process conditions. The method for producing polyolefin with strong robustness provided by the present invention will be described in detail with reference to specific examples.
Example 1
According to production mode I, the two main reactors 104/105 are operated in parallel and the reaction product is a polyolefin elastomer.
The second control valve 2, the third control valve 3, the fourth control valve 4 and the eighth control valve 8 are closed, the temperature of the first alpha-olefin monomer in the raw material feeding pipe 001 is controlled at 35 ℃ after passing through the feeding heat exchanger 101, and the first alpha-olefin monomer is split into two parts. Wherein a first alpha-olefin monomer enters the prepolymerization reactor 102 together with a main catalyst in a main catalyst feed pipe 002 and a co-catalyst in a co-catalyst feed pipe 003, the prepolymerization reactor 102 having the function of diluting and buffering the catalyst in this embodiment. The mixed mixture flow was passed through a pipe and a transfer pump 103 to two main reactors 104/105, at which time the two main reactors 104/105 were controlled to a temperature of 92℃and a pressure of 1.8MPa. Another first α -olefin monomer is fed into the hybrid refiner 112 through the first control valve 1 and is mixed and refined with a second α -olefin monomer fed into the hybrid refiner 112 through the refiner feed pipe 007, and the mixed stream is fed to the buffer tank 113, at which time the buffer tank 113 is operated at a temperature of 32 ℃ and at a pressure of 2.5MPa. The mixture then flows through the fifth control valve 5 by means of a transfer pump 114, is warmed to 55 ℃ by means of a heat exchanger 115 and is transferred to the two main reactors 104/105. After the reaction is completed, the reaction product is conveyed to the plant boundary region via a sixth control valve 6.
To control the reaction intensity and product quality, the two main reactors 104/105 were operated in semi-continuous form with a feed time of about 1.5 hours and a reaction time of about 2.5 hours.
The utility flow introduced into the temperature control loop 017 is a heating medium, the two main reactors 104/105 provide heat in the reaction process by the utility flow, and the gas phase flow in the reaction process can be conveyed to the top cooler 106/109 through a pipeline for temperature regulation and control, the cooled flow is conveyed to the top reflux tank 107/110, the operating temperature is 45 ℃, the operating pressure is 1.8MPa, the reflux liquid is boosted by the conveying pump 108/111 and then enters the two main reactors 104/105, and the accurate regulation and control of the temperature in the two main reactors 104/105 are completed.
Example 2
According to production mode II, the two main reactors 104/105 are operated in series and the reaction product is a homopolymer.
The first control valve 1 and the sixth control valve 6 are closed, and the first alpha-olefin monomer in the raw material feeding pipe 001 is split into two after passing through the feeding heat exchanger 101, and the temperature is controlled below 20 ℃. One of the first alpha-olefin monomers enters the prepolymerizer 102 with a main catalyst in main catalyst feed line 002 and a co-catalyst in co-catalyst feed line 003. In this embodiment, the prepolymerizer 102 has dilution and prepolymerization. The mixed mixture flow is fed to the first main reactor 104 through a pipe and a transfer pump 103, while another strand of the first alpha-olefin monomer is fed directly into the first main reactor 104 through the second control valve 2 and the pipe. The reaction temperature of the first main reactor 104 was 70℃and the reaction pressure was 3.3MPa. After closing the seventh control valve 7 and opening the eighth control valve 8, the semi-finished product enters the second main reactor 105 from the first main reactor 104, the reaction temperature of the second main reactor 105 is 75 ℃, and the reaction pressure is 3.5MPa. At this time, the first main reactor 104 and the second main reactor 105 were operated in batch mode for 2 hours and 1.5 hours, respectively.
The utility stream fed into the temperature control loop 017 serves as a heating function during the initial stages of the reaction and is changed to a cooling medium when the reaction is warmed to the operating temperature of the first main reactor 104. The gas phase material flows of the two main reactors 104/105 in the reaction process can be conveyed to the top cooler 106/109 for temperature regulation, the cooled material flows to the top reflux tank 107/110, the operating temperatures of the top cooler 106/109 and the top reflux tank 107/110 are 35 ℃ and 40 ℃, and the operating pressures are 3.2MPa and 3.4MPa respectively; the reflux liquid enters the two main reactors 104/105 after being boosted by the delivery pump 108/111, and the accurate regulation and control of the temperature in the reactors are completed.
The reaction product was fed into the hybrid refiner 112 through the third control valve 3 while the modifier was fed into the hybrid refiner 112 through the refiner feed pipe 007, and the mixture stream was fed to the buffer tank 113 at an operating temperature of 71 c and an operating pressure of 2.0MPa in the buffer tank 113. The reaction product is conveyed to the equipment boundary region through a conveying pump 114 and a fourth control valve 4, or when the product is failed, the reaction product is heated through a heat exchanger 115 and then returned to the first reactor 104.
Example 3
According to production mode I, the two main reactors 104/105 are operated in series and the reaction product is a polyolefin elastomer.
Similar to example 1, the first alpha-olefin monomer in feed line 001 passed through feed heat exchanger 101 and then entered prepolymerization reactor 102 with a main catalyst in main catalyst feed line 002 and a co-catalyst in co-catalyst feed line 003. The mixture flow was fed to the first main reactor 104 through a pipe and a transfer pump 103, and the reaction temperature of the first main reactor 104 was 85℃and the reaction pressure was 1.5MPa. After closing the seventh control valve 7 and opening the eighth control valve 8, the semi-finished product enters the second main reactor 105 from the first main reactor 104, the reaction temperature of the second main reactor 105 is 95 ℃, and the reaction pressure is 1.8MPa. At this point, the first main reactor 104 was operated in a semi-continuous mode with a reaction time of 1.5 hours; the second main reactor 105 was operated as a batch and the reaction time was 1 hour. The reaction products are fed to the plant limits via a sixth control valve 6.
The second alpha-olefin monomer may be added according to the product requirement, i.e. by closing the second control valve 2, feeding the second alpha-olefin monomer through the refiner feed pipe 007, mixing with the semi-finished product output from the first main reactor 104, and then adding the mixture to the second main reactor 105 at one time.
Example 4
According to production mode II, the two main reactors 104/105 are operated in parallel and the reaction product is a copolymer.
The first control valve 1, the fourth control valve 4 and the sixth control valve 6 are closed, the temperature of the first alpha-olefin monomer in the raw material feeding pipe 001 is controlled at 80 ℃ after passing through the feeding heat exchanger 101, and the temperature is split into two streams. One of the first alpha-olefin monomers enters the prepolymerizer 102 with a main catalyst in the main catalyst feed line 002 and a co-catalyst in the co-catalyst feed line 003. In this embodiment, the prepolymerizer 102 has a prepolymerization with a residence time of 18 minutes. The mixed mixture flow is sent to a first main reactor 104 through a pipeline and a delivery pump 103; simultaneously, the other strand of the first alpha-olefin monomer also directly enters the first main reactor 104 through the second control valve 2 and the pipeline, and the reaction temperature of the first main reactor 104 is 90 ℃ and the reaction pressure is 2.2MPa.
The utility stream fed into the temperature control loop 017 is a heating medium that provides initial energy for the reaction. The gas phase material flow in the reaction process can be conveyed to the top cooler 106 through a pipeline for temperature regulation and control, the cooled material flow is conveyed to the top reflux tank 107, the operating temperature of the top reflux tank 107 is 35 ℃, the operating pressure is 2.2MPa, the reflux liquid is boosted by the conveying pump 108 and then returned to the first main reactor 104, the accurate regulation and control of the temperature in the reactor is completed, and the reaction time of the first main reactor 104 is 1 hour.
When the two reaction kettles are connected in parallel, the eighth control valve 8 is closed, the seventh control valve 7 is opened, the semi-finished product enters the mixing refiner 112 from the first main reactor 104 through the third control valve 3, the second alpha-olefin monomer enters the mixing refiner 112 from the refiner feed pipe 007, and the mixture flow is conveyed to the buffer tank 113, wherein the operation temperature of the buffer tank 113 is 90 ℃ and the operation pressure is 2.1MPa. The mixture stream was then passed through a pipe and transfer pump 114 with a pressure rise to 3.0MPa, a temperature rise to 110 c through a fifth control valve 5 and heat exchanger 115, and finally transferred to the second main reactor 105 with an operating temperature of 135 c and an operating pressure of 2.8MPa for the second main reactor 105. The utility stream introduced into the temperature control loop 017 of the second main reactor 105 is a cooling medium, and at the same time, the gas phase stream in the reaction process can be transported to the top cooler 109 through a pipeline to perform temperature regulation, the cooled gas phase stream is transported to the top reflux drum 110, the operation temperature is 40 ℃, the operation pressure is 2.8MPa, the reflux liquid is returned to the second main reactor 105 after being boosted by the transfer pump 111, and the reaction time is about 70 minutes. At this point, the seventh control valve 7 and the third control valve 3 are closed and the reaction product is fed to the plant boundary region via the sixth control valve 6.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.
Claims (10)
1. A polyolefin production plant with strong robustness, characterized by comprising a prepolymerization reactor (102), a main reactor set, a hybrid refiner (112) and a buffer tank (113);
the raw material feeding pipe (001) is divided into two branches, wherein one branch is connected with the main reactor group through a second control valve (2) and is connected with the mixing refiner (112) through a first control valve (1); the other branch is connected with a main catalyst feeding pipe (002) and an auxiliary catalyst feeding pipe (003) to a prepolymerization reactor (102), and the prepolymerization reactor (102) is connected with a main reactor group;
The discharge channel of the main reactor group is divided into two branches, wherein one branch is connected to the device boundary region through a sixth control valve (6); the other branch is connected with the mixing refiner (112) through a third control valve (3); the mixing refiner (112) is also connected with a refiner feed pipe (007); the discharging channel of the mixing refiner (112) is connected with a buffer tank (113);
the discharging channel of the buffer tank (113) is divided into two branches, wherein one branch is connected to the device boundary region through a fourth control valve (4), and the other branch is connected with the main reactor group through a fifth control valve (5);
A temperature control loop (017) is arranged on the main reactor group.
2. The polyolefin production apparatus of claim 1, wherein the primary reactor set comprises at least two primary reactors;
Preferably, the main reactors are connected in series or parallel; and/or the main reactor is a stirred tank reactor or a loop reactor.
3. The polyolefin production plant of claim 1 or 2, further comprising a top cooling device connected to the main reactor set; preferably, the top cooling device comprises a top cooler and a top reflux drum;
and/or the main reactor group is connected with a modifier feeding pipe (004).
4. A process for producing a polyolefin with strong robustness for use in a polyolefin production plant according to any of claims 1-3, characterized in that the process for producing a polyolefin is switchable between two production modes, production mode i and production mode ii, depending on the raw material and product scheme:
Production mode i includes:
The first alpha-olefin monomer in the raw material feeding pipe (001) is split into two streams, wherein one stream of the first alpha-olefin monomer is conveyed to the prepolymerization reactor (102) to be mixed together with the main catalyst in the main catalyst feeding pipe (002) and the auxiliary catalyst in the auxiliary catalyst feeding pipe (003), and the mixed stream is conveyed to the main reactor group;
The other first alpha-olefin monomer is delivered to a hybrid refiner (112), while the optional second alpha-olefin monomer or solvent is also delivered to the hybrid refiner (112) through a refiner feed tube (007), and the stream output from the hybrid refiner (112) is delivered to a buffer tank (113) and from the buffer tank (113) to the main reactor set;
after the reaction in the main reactor group is finished, the reaction product is discharged and conveyed to a device boundary region;
Production mode ii includes:
The first alpha-olefin monomer in the raw material feeding pipe (001) is split into two streams, wherein one stream of the first alpha-olefin monomer is conveyed to the prepolymerization reactor (102) to be mixed together with the main catalyst in the main catalyst feeding pipe (002) and the auxiliary catalyst in the auxiliary catalyst feeding pipe (003), and the mixed stream is conveyed to the main reactor group;
another stream of the first alpha-olefin monomer is directly fed to the main reactor set;
after the reaction in the main reactor set is completed, the reaction product is conveyed to a hybrid refiner (112), and simultaneously, optional second alpha-olefin monomer, solvent or modifier is also conveyed to the hybrid refiner (112) through a refiner feed pipe (007), the material flow output by the hybrid refiner (112) is conveyed to a buffer tank (113), after settling separation, part of the product is conveyed to a device boundary zone, and the other part of solvent, unreacted monomer or unreacted complete polymer is conveyed back to the main reactor set.
5. The process for producing polyolefin according to claim 4, wherein the production mode I further comprises: the modifier is directly conveyed to the main reactor group through a modifier feeding pipe (004);
And/or, production mode ii further comprises: the modifier is directly conveyed to the main reactor group through a modifier feeding pipe (004).
6. A polyolefin production process according to claim 4 or 5, wherein the main reactor group is temperature controlled by passing a utility stream into the temperature control loop (017);
And/or the gas phase stream in the main reactor set is sent to an overhead cooler for cooling and then to an overhead reflux drum and back to the main reactor set.
7. The method according to any one of claims 4 to 6, wherein the main reactor set is operated in any one of continuous operation, batch operation, semi-continuous operation, and the operation period is any one of linear, stepped, or wave-shaped.
8. The polyolefin production process according to any of claims 4 to 7, wherein the reaction temperature of the prepolymerization reactor (102) is 30 to 100 ℃, the operating pressure is 0.5 to 4.5MPa, and the reaction time is 1 to 60min;
And/or the reaction temperature of the main reactor group is 50-150 ℃, the operation pressure is 0.5-4.5 MPa, the reaction time is 30-240 min, the operation liquid level is 50-90%, and the stirring speed is 30-150 r/min;
and/or the operating temperature of the top cooler is 20-60 ℃ and the operating pressure is 0.5-4.5 MPa;
and/or the operating temperature of the top reflux tank is 20-60 ℃ and the operating pressure is 0.5-4.5 MPa;
and/or the operation temperature of the mixing refiner (112) is 20-150 ℃ and the operation pressure is 0.5-4 MPa;
And/or the operation temperature of the buffer tank (113) is 30-200 ℃, the operation pressure is 0.5-4 MPa, and the residence time is 5-100 min.
9. The polyolefin production process of any of claims 4-8, wherein the first α -olefin monomer comprises at least one of ethylene, propylene, 1-butene, 1-hexene, and 1-octene;
And/or the second alpha-olefin monomer comprises at least one of ethylene, propylene, 1-butene, 1-hexene, and 1-octene.
10. The polyolefin production process according to any of claims 4 to 9, wherein the procatalyst comprises at least one catalyst precursor, at least one activator and optionally at least one catalyst support;
and/or the modifier comprises at least one of antistatic agent, chain transfer agent, condensing agent and inert gas.
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| CN202211314175.0A CN117924570A (en) | 2022-10-25 | 2022-10-25 | Polyolefin production device and method with strong robustness |
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| CN202211314175.0A CN117924570A (en) | 2022-10-25 | 2022-10-25 | Polyolefin production device and method with strong robustness |
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| CN202211314175.0A Pending CN117924570A (en) | 2022-10-25 | 2022-10-25 | Polyolefin production device and method with strong robustness |
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