CN111939846B - Device and method for synthesizing poly alpha-olefin - Google Patents
Device and method for synthesizing poly alpha-olefin Download PDFInfo
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- CN111939846B CN111939846B CN201910414861.7A CN201910414861A CN111939846B CN 111939846 B CN111939846 B CN 111939846B CN 201910414861 A CN201910414861 A CN 201910414861A CN 111939846 B CN111939846 B CN 111939846B
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- 229920013639 polyalphaolefin Polymers 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 15
- 239000003507 refrigerant Substances 0.000 claims abstract description 47
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 238000000605 extraction Methods 0.000 claims abstract description 4
- 239000003054 catalyst Substances 0.000 claims description 53
- 239000004711 α-olefin Substances 0.000 claims description 26
- 239000002002 slurry Substances 0.000 claims description 22
- 238000006116 polymerization reaction Methods 0.000 claims description 21
- 239000002994 raw material Substances 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 15
- AFFLGGQVNFXPEV-UHFFFAOYSA-N 1-decene Chemical compound CCCCCCCCC=C AFFLGGQVNFXPEV-UHFFFAOYSA-N 0.000 claims description 13
- 238000002156 mixing Methods 0.000 claims description 9
- 239000012752 auxiliary agent Substances 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 3
- 238000011031 large-scale manufacturing process Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 27
- 239000002199 base oil Substances 0.000 description 3
- CRSBERNSMYQZNG-UHFFFAOYSA-N 1 -dodecene Natural products CCCCCCCCCCC=C CRSBERNSMYQZNG-UHFFFAOYSA-N 0.000 description 2
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229940069096 dodecene Drugs 0.000 description 2
- 239000010687 lubricating oil Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000010538 cationic polymerization reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 239000000539 dimer Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000006384 oligomerization reaction Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000013638 trimer Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
- C07C2/08—Catalytic processes
- C07C2/14—Catalytic processes with inorganic acids; with salts or anhydrides of acids
- C07C2/20—Acids of halogen; Salts thereof ; Complexes thereof with organic compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/06—Halogens; Compounds thereof
- C07C2527/08—Halides
- C07C2527/12—Fluorides
- C07C2527/1213—Boron fluoride
Abstract
The invention belongs to the field of chemical industry, and particularly discloses a device and a method for synthesizing poly-alpha-olefin. The device is a device capable of automatically maintaining the reaction temperature in the PAO reactor to be constant, avoids the over-high or over-low temperature in the reaction process, improves the yield of the target product, and further meets the requirement of large-scale reactor. Compared with the prior art, the device for synthesizing the poly-alpha-olefin can realize large-scale production of the poly-alpha-olefin (PAO), has higher heat transfer coefficient in the reactor, can accurately control the reaction temperature by controlling the amount of the refrigerant and the heat extraction area, and effectively prevents the reaction from being over-heated.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a device and a method for synthesizing poly alpha-olefin.
Background
Poly-Alpha-olefins (PAO) are one of the most commonly used synthetic lubricant base oils, and are derived from linear Alpha-olefins (C) 6 -C 14 Alpha-olefin monomer or mixed olefin) to form a dimer, trimer, tetramer, etc. The PAO has the characteristics of high viscosity index, low pour point, low volatility, high flash point, good thermal oxidation stability, excellent high and low temperature performance, long service life and the like, is ideal base oil for preparing high-grade and special lubricating oil, and is widely applied to the industries of aerospace, military, transportation, cosmetics and the like. PAO (poly-alpha-olefin) synthetic oil (PAO for short) has good viscosity-temperature performance and low-temperature fluidity, is ideal base oil for preparing high-grade and special lubricating oil, is called polydecene if the raw material alpha-olefin is decene or dodecene if the raw material alpha-olefin is dodecene, and can be divided into low viscosity (2-10 cSt) and high viscosity (PAO) according to viscosity>25 cSt) two major markets. The difference in viscosity is due to the length of the polymerization and the difference in the starting alpha-olefins.
The oligomerization cationic polymerization reaction of the alpha-olefin is an exothermic reaction, the exothermic amount is not uniform, the instantaneous exothermic amount is large, the exothermic amount is gradually reduced, the reaction temperature needs to be strictly controlled in a certain interval, and other polymers can be generated by the reaction when the temperature is too high or too low, so that the control of the temperature of the reactor is the biggest difficulty.
At present, methods for strictly controlling the reaction temperature of the PAO reactor are rarely reported. The reaction temperature of the target reaction is controlled to be constant, the phenomenon that the temperature is too high or too low in the reaction process is avoided, the yield of the target product is improved, the requirement of large-scale reactor is met, and the problem to be solved in the technical field of PAO is urgently solved.
Disclosure of Invention
The invention aims to provide a device capable of automatically maintaining the reaction temperature in a PAO reactor constant, avoiding the over-high or over-low temperature in the reaction process, improving the yield of a target product and further meeting the requirement of large-scale reactor.
In order to achieve the above objects, the present invention provides an apparatus for synthesizing polyalphaolefin, comprising one or more slurry bed reactors connected in series, wherein the slurry bed reactor comprises an upper head, a barrel and a lower head;
a product outlet is formed in the upper end enclosure;
the cylinder is provided with a refrigerant outlet and a refrigerant inlet, the cylinder is internally provided with a heat-taking coil pipe, the heat-taking coil pipe is respectively connected with the refrigerant outlet and the refrigerant inlet, and a pipeline where the refrigerant outlet is located is provided with a temperature control system for adjusting the flow of the refrigerant outlet according to the temperature of a product outlet;
the lower end enclosure is provided with a feed inlet and an excessive catalyst inlet, the feed inlet is connected with a feed collection pipeline, and the feed collection pipeline is respectively connected with a raw material feed pipeline and a catalyst feed pipeline;
the product outlet of the first stage slurry bed reactor is connected with a product extraction pipeline or a raw material feeding pipeline of the next stage slurry bed reactor;
the lower part of the heat taking coil pipe is sequentially provided with a gas-liquid distribution disc and a gas distributor, and the gas distributor is connected with the excessive catalyst inlet.
In order to uniformly distribute the liquid and the gas and enhance the mixing of the liquid and the gas, in the invention, preferably, a plurality of gas-liquid distributors are arranged on the gas-liquid distribution disc, and the gas-liquid distributors are hood-type gas-collecting distributors and/or distribution holes; preferably, the hood-type gas collecting distributor and/or the distribution holes are 20-200 and are arranged in a square or triangle shape.
In the invention, in order to mix the excessive catalyst, the raw materials in the reactor and the catalyst more uniformly, the gas distributor selected in the invention is preferably a perforated pipe, the diameter of the perforated pipe is 1-15 mm, the perforated pipe can be circular, dendritic, fishbone-shaped and the like, and the porous pipe can be selected by a person skilled in the art according to experience.
In the invention, in order to remove the reaction heat in the reactor more efficiently and timely, a plurality of groups of heat-taking coils can be arranged, preferably 2-10 groups, and the heat-taking coils are conventional high-flux tubes or finned tubes.
In another aspect, the present invention provides a process for the synthesis of polyalphaolefins, carried out in the above apparatus, said process comprising:
alpha-olefin from a raw material feeding pipeline and a catalyst from a catalyst feeding pipeline are preliminarily mixed in a feeding collecting pipeline and then enter the bottom of the slurry bed reactor through a feeding hole, the alpha-olefin and the catalyst are mixed with an excessive catalyst from a gas distributor and undergo a polymerization reaction, a product of the polymerization reaction is extracted through a product outlet or is sent to the feeding hole of the next-stage slurry bed reactor, heat generated by the polymerization reaction is removed through heat exchange with a refrigerant in a heat taking coil pipe, and the flow of the refrigerant outlet is adjusted according to the temperature of the product outlet.
In the present invention, in order to reduce the reaction of α -olefin in the region without heat removal means, it is preferable that the temperature of the preliminary mixing is less than 15 ℃, since the temperature of the preliminary mixing is less than 15 ℃ and does not reach the reaction temperature of polymerization, the preliminary mixing process of α -olefin and catalyst does not generate heat, and heat removal is not necessary. After the preliminary mixing, in order to initiate the polymerization reaction, it is preferable that the temperature of the excess catalyst is 40 to 100 ℃, the temperature of the α -olefin, the catalyst and the excess catalyst after mixing is 15 to 55 ℃, and the pressure in the reactor is controlled by the excess catalyst.
According to the present invention, preferably, the pressure of the polymerization reaction is 0.01 to 0.75MPaG; the temperature is 15-55 ℃, preferably 20-30 ℃; the reaction residence time is 0.9 to 9 hours; the mass ratio of the alpha-olefin to the catalyst to the excess catalyst is 1:0.003 to 0.04: 0.003-0.01.
According to the present invention, preferably, the alpha-olefin is C 8 ～C 12 Preferably the alpha-olefin comprises 1-decene, said 1-decene content being greater than 55mol%.
According to the invention, preferably, the catalyst comprises a main catalyst and an auxiliary agent, wherein the main catalyst is BF 3 、AlCl 3 、TiCl 4 、SnCl 4 At least one of (a); the auxiliary agent is a proton donor, and the proton donor is preferably water or C 2 -C 8 At least one of alpha-monoalcohols.
The heat released by the reaction is removed out of the reactor through heat exchange with the refrigerant in the heat taking coil, the refrigerant can be pure substances, the heat is taken by evaporation of the refrigerant, and preferably, after heat exchange, the gas-liquid phase mass ratio of the refrigerant in the heat taking coil is 1:4 to 20. In the heat exchange process, the flow of a refrigerant outlet is adjusted according to the temperature of a product outlet, and when the temperature of the product outlet is increased, the raw materials participating in the polymerization reaction are increased, and the refrigerant needs to be supplemented in time; when the product outlet temperature is lowered, it means that the amount of the raw material participating in the polymerization reaction is decreased, and the amount of the injected refrigerant needs to be decreased. In the present invention, it is preferable that the temperature of the product outlet after the heat exchange is maintained at 25 to 35 ℃.
Compared with the prior art, the device for synthesizing the poly-alpha-olefin can realize large-scale production of the poly-alpha-olefin (PAO), has higher heat transfer coefficient in the reactor, can accurately control the reaction temperature by controlling the amount of the refrigerant and the heat extraction area, and effectively prevents the reaction from being over-heated.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings, wherein like reference numerals generally represent like parts in the exemplary embodiments of the present invention.
FIG. 1 shows a schematic process flow diagram for a single apparatus for synthesizing polyalphaolefins according to one embodiment of the present invention.
FIG. 2 shows a schematic of a gas distributor according to one embodiment of the present invention.
FIG. 3 shows a schematic process flow diagram of a plant for the series synthesis of polyalphaolefins according to one embodiment of the present invention.
Description of reference numerals:
1. a slurry bed reactor; 2. a feed inlet; 3. an excess catalyst inlet; 4. catalyst and auxiliary agent inlet pipes; 5. a product outlet; 6. a refrigerant inlet; 7. a refrigerant outlet; 8. a heat-taking coil pipe; 9. a gas-liquid distribution disc; 10. a gas distributor; 11. a temperature control system; 12. a barrel; 13. an upper end enclosure; 14. sealing the end;
s-1, alpha-olefin; s-2, a catalyst; s-3, excess catalyst; s-4, reaction products; s-5, cooling media; and S-6, heat exchange is carried out on the refrigerant.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
Example 1
Apparatus for synthesizing polyalphaolefin:
the device comprises a slurry bed reactor 1, wherein the slurry bed reactor 1 comprises an upper end enclosure 13, a cylinder 12 and a lower end enclosure 14;
the upper end enclosure 13 is provided with a product outlet 5; a refrigerant outlet 7 and a refrigerant inlet 6 are arranged on the cylinder 12, 10 groups of heat-taking coil pipes 8 are arranged in the cylinder 12, the heat-taking coil pipes 8 are respectively connected with the refrigerant outlet 7 and the refrigerant inlet 6, and a temperature control system 11 is arranged on a pipeline where the refrigerant outlet 7 is located and used for adjusting the flow of the refrigerant outlet according to the temperature of a product outlet; the lower end enclosure 14 is provided with a feed inlet 2 and an excessive catalyst inlet 3, the feed inlet 2 is connected with a feed collection pipeline, and the feed collection pipeline is respectively connected with a raw material feed pipeline and a catalyst feed pipeline; the lower part of the heat taking coil 8 is sequentially provided with a gas-liquid distribution disc 9 and a gas distributor 10, and the gas distributor 10 is connected with the excessive catalyst inlet 3; 200 distribution holes which are arranged in a triangular shape are arranged on the gas-liquid distribution disk 9; the gas distributor (shown in FIG. 2) is a perforated tube with a diameter of 15mm.
The process flow for synthesizing the poly-alpha-olefin by using the device is shown in figure 1:
the alpha-olefin S-1 from a raw material feeding pipeline and the catalyst S-2 from a catalyst feeding pipeline are preliminarily mixed in a feeding collection pipeline, then enter the bottom of a slurry bed reactor 1 through a feeding hole 2, and are mixed with an excessive catalyst S-3 from a gas distributor 10 to carry out a polymerization reaction, wherein the alpha-olefin is 1-decene, and the mass ratio of the alpha-olefin to the catalyst to the excessive catalyst is 1:0.003 to 0.04:0.003 to 0.01, the temperature of the primary mixing is less than 15 ℃, and the temperature of the excessive catalyst is 40 to 100 ℃; the temperature of a product outlet is 25-35 ℃, after heat exchange, the gas-liquid phase mass ratio of the refrigerant in the heat taking coil is 1:4 to 20. The pressure of the polymerization reaction is 0.01-0.75 MPaG; the temperature is 20-30 ℃; the reaction residence time is 0.9 to 9 hours, and the main catalyst is BF 3 The assistant is water.
The product of the polymerization reaction is extracted through the product outlet 5, the heat generated by the polymerization reaction is transferred out through the heat exchange with the refrigerant in the heat-extracting coil 8, and the flow of the refrigerant outlet 7 is adjusted according to the temperature of the product outlet 5.
Example 2
Apparatus for synthesizing polyalphaolefin:
the device comprises two slurry bed reactors 1 connected in series, wherein each slurry bed reactor 1 comprises an upper end enclosure 13, a cylinder 12 and a lower end enclosure 14;
the upper end enclosure 13 is provided with a product outlet 5; a refrigerant outlet 7 and a refrigerant inlet 6 are arranged on the cylinder 12, 2 groups of heat-taking coil pipes 8 are arranged in the cylinder 12, the heat-taking coil pipes 8 are respectively connected with the refrigerant outlet 7 and the refrigerant inlet 6, and a temperature control system 11 is arranged on a pipeline where the refrigerant outlet 7 is positioned and used for adjusting the flow of the refrigerant outlet according to the temperature of a product outlet; the lower end enclosure 14 is provided with a feed inlet 2 and an excessive catalyst inlet 3, the feed inlet 2 is connected with a feed collection pipeline, and the feed collection pipeline is respectively connected with a raw material feed pipeline and a catalyst feed pipeline; the lower part of the heat taking coil 8 is sequentially provided with a gas-liquid distribution disc 9 and a gas distributor 10, and the gas distributor 10 is connected with the excessive catalyst inlet 3; 20 hood-type gas collecting distributors arranged in a square shape are arranged on the gas-liquid distribution disk 9; the gas distributor (shown in FIG. 2) is a perforated tube with a diameter of 1 mm; the product outlet of the first stage slurry bed reactor is connected with the raw material feeding pipeline of the second stage slurry bed reactor.
The process flow for synthesizing the poly-alpha-olefin by using the device is shown in figure 3:
alpha-olefin S-1 from a raw material feeding pipeline and catalyst S-2 from a catalyst feeding pipeline are preliminarily mixed in a feeding collection pipeline, then enter the bottom of a slurry bed reactor 1 through a feeding hole 2, are mixed with excessive catalyst S-3 from a gas distributor 10 and have a polymerization reaction, wherein the alpha-olefin is 1-decene, and the mass ratio of the alpha-olefin to the catalyst to the excessive catalyst is 1:0.003 to 0.04:0.003 to 0.01, the temperature of the primary mixing is less than 15 ℃, and the temperature of the excessive catalyst is 40 to 100 ℃; the temperature of a product outlet is 25-35 ℃, and after heat exchange, the gas-liquid phase mass ratio of the refrigerant in the heat taking coil is 1:4 to 20. The pressure of the polymerization reaction is 0.01-0.75 MPaG; the temperature is 20-30 ℃; the reaction residence time is 0.9 to 9 hours, and the main catalyst is BF 3 The assistant is water.
The product of the polymerization reaction is sent to the feed inlet of the second-stage slurry bed reactor through the product outlet 5, the heat generated by the polymerization reaction is removed through heat exchange with the refrigerant in the heat taking coil 8, and the flow of the refrigerant outlet 7 is adjusted according to the temperature of the product outlet.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (11)
1. A process for synthesizing polyalphaolefins, wherein the process is carried out in an apparatus for synthesizing polyalphaolefins, said process comprising:
alpha-olefin from a raw material feeding pipeline and a catalyst from a catalyst feeding pipeline are preliminarily mixed in a feeding collecting pipeline, then enter the bottom of the slurry bed reactor through a feeding hole, are mixed with an excessive catalyst from a gas distributor and are subjected to a polymerization reaction, a product of the polymerization reaction is extracted through a product outlet or is sent to the feeding hole of the next stage of slurry bed reactor, heat generated by the polymerization reaction is removed through heat exchange with a refrigerant in a heat taking coil pipe, and the flow of the refrigerant outlet is adjusted according to the temperature of the product outlet;
the temperature of the preliminary mixing is less than 15 ℃, and the temperature of the excessive catalyst is 40-100 ℃; the temperature of the product outlet is 25 to 35 ℃;
the device for synthesizing the poly-alpha-olefin comprises one or more slurry bed reactors connected in series, wherein each slurry bed reactor comprises an upper end enclosure, a cylinder and a lower end enclosure;
a product outlet is formed in the upper end enclosure;
the cylinder is provided with a refrigerant outlet and a refrigerant inlet, the cylinder is internally provided with a heat-taking coil pipe, the heat-taking coil pipe is respectively connected with the refrigerant outlet and the refrigerant inlet, and a pipeline where the refrigerant outlet is located is provided with a temperature control system for adjusting the flow of the refrigerant outlet according to the temperature of a product outlet;
the lower end enclosure is provided with a feed inlet and an excessive catalyst inlet, the feed inlet is connected with a feed collection pipeline, and the feed collection pipeline is respectively connected with a raw material feed pipeline and a catalyst feed pipeline;
the product outlet of the first stage slurry bed reactor is connected with a product extraction pipeline or a raw material feeding pipeline of the next stage slurry bed reactor;
the lower part of the heat taking coil is sequentially provided with a gas-liquid distribution disc and a gas distributor, and the gas distributor is connected with the excessive catalyst inlet;
the heat taking coil pipes are 2-10 groups.
2. The method of claim 1, wherein a plurality of gas-liquid distributors are arranged on the gas-liquid distribution disc, and the gas-liquid distributors are hood-type gas-collecting distributors and/or distribution holes.
3. The method according to claim 2, wherein the hood-type gas collecting distributor and/or the distribution holes are 20 to 200 and arranged in a square or triangle.
4. The method of claim 1, wherein the gas distributor is a perforated pipe having a diameter of 1 to 15mm.
5. The method as claimed in claim 1, wherein after heat exchange, the refrigerant in the heat-taking coil has a gas-liquid phase mass ratio of 1:4 to 20.
6. The process according to claim 1, wherein the polymerization is carried out at a pressure of 0.01 to 0.75MPaG; the temperature is 15 to 55 ℃; the reaction residence time is 0.9 to 9h; the mass ratio of the alpha-olefin to the catalyst to the excess catalyst is 1:0.003 to 0.04:0.003 to 0.01.
7. The method according to claim 6, wherein the temperature is 20 to 30 ℃.
8. The method of claim 1, wherein the alpha olefin is C 8 ~C 12 At least one of alpha-olefins (b) of (a).
9. The method of claim 8, wherein the alpha-olefin comprises 1-decene, and wherein the 1-decene content is greater than 55mol%.
10. The method of claim 1, wherein the catalyst comprises a procatalyst and a cocatalyst, the procatalyst being BF 3 、AlCl 3 、TiCl 4 、SnCl 4 At least one of; the auxiliary agent is a proton donor.
11. The method of claim 10, wherein the proton donor is water, C 2 -C 8 At least one of alpha-monoalcohols.
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| ATE507247T1 (en) * | 1999-09-16 | 2011-05-15 | Tpc Group Llc | METHOD FOR PRODUCING POLYOLEFIN PRODUCTS |
| US8389751B2 (en) * | 2009-04-21 | 2013-03-05 | Dow Technology Investments Llc | Simplified method for producing alkylene oxides with a high efficiency catalyst as it ages |
| US10058838B2 (en) * | 2013-12-11 | 2018-08-28 | Sasol Technology Proprietary Limited | Method of shutting down an operating three-phase slurry bubble column reactor |
| CN109593151B (en) * | 2017-09-30 | 2022-04-08 | 中国石油化工股份有限公司 | Process and system for producing polyalphaolefin, polyalphaolefin and continuous reactor |
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| CN101402541A (en) * | 2008-11-21 | 2009-04-08 | 清华大学 | Fluidized bed process and apparatus for producing ethylene with acetylene hydrogenation |
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| CN107089917A (en) * | 2017-05-26 | 2017-08-25 | 清华大学 | Multiple stage fluidized-bed middle nitrobenzene compounds Hydrogenation for amino benzenes compounds technique |
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