RU2809822C1 - Installation and method for obtaining polyalphaolefins - Google Patents

Abstract

FIELD: polyalphaolefins.

SUBSTANCE: invention relates to a plant for the production of polyalphaolefins, including an inlet unit (1), a microchannel reactor (2) and a post-processing unit (3), which are connected in series, wherein the inlet unit includes a mixer and/or pipeline(s) for supplying olefin feed material, auxiliary raw materials and BF₃ catalyst into a microchannel reactor (2), the inlet unit (1) contains at least a mixer for mixing at least a part of the auxiliary raw materials and at least a part of the BF₃ catalyst and a pipeline for separate supplying at least part of the BF₃ catalyst to the microchannel reactor (2). The invention also relates to a method.

EFFECT: use of the proposed invention makes it possible to obtain alpha-olefin oligomers with high conversion, high selectivity, simplicity of the process, low capital investment, as well as safety and environmental friendliness.

17 cl, 16 tbl, 8 ex, 7 dwg

Description

Field of technology

The present invention relates to a plant and method for producing polyalphaolefins, in particular to a plant and method for producing polyalphaolefins using a microchannel reactor.

State of the art

Polyalphaolefins are typically produced by the polymerization of one or more linear alpha-olefins through an oligomerization reaction under the influence of catalysts. Hydrogenated polyalphaolefins, obtained by separating and hydrogenating polyalphaolefins, can be used for blending into high quality synthetic base oils. Polyalpha olefin synthetic base oil, also known as PAO synthetic base oil, has excellent properties such as high viscosity index, ultra-low pour point, excellent thermal and oxidative stability and high flash point, so it is widely used. PAO synthetic base oils are classified according to their kinematic viscosities at 100°C. Main products include PAO4, PAO6, PAO8, PAO10, PAO40, PAO100, etc. Of these, low-viscosity PAOs with a kinematic viscosity at 100°C between 4 and 8 cSt are the most widely used, mainly for mixing with various types of high-quality motor oils. The use of low-viscosity PAOs can reduce engine torque loss when cold, while extending oil drain intervals and improving fuel economy.

The traditional process for producing polyalphaolefins generally uses a Lewis acid catalytic system to subject the alpha olefins to an oligomerization reaction, and the reaction will produce polymers with varying degrees of polymerization. Currently, the catalysts used in industry for the production of low-viscosity polyalphaolefins are mainly BF ₃ -(excipient) catalysts. Typical production methods use batch or continuous mixing reactors. In an oligomerization reaction system in which alpha-olefins catalyze BF ₃ -(excipient), the BF ₃ in the gas phase must be completely dispersed and mixed with the excipient and alpha-olefins in the liquid phase, with a portion of it dissolving to form the active cationic catalyst and then initiates the alpha-olefin oligomerization reaction. BF ₃ dissolution and interfacial mass transfer determine the macroscopic reaction rate, conversion, etc. In addition, if the reaction time is too short, olefin conversion is generally low and product yield is low. If the reaction time is too long, the resulting alpha-olefin oligomer may undergo side reactions such as a secondary polymerization reaction, which increases the degree of polymerization, and an isomerization reaction, which causes a decrease in viscosity index.

US4045508A discloses a process for the continuous production of polyalphaolefins, which is characterized by combining a mixing reactor and a tubular reactor to control a multi-stage polymerization process. However, this method leads to a large secondary polymerization reaction of oligomers, and the trimer content is significantly reduced.

Document CN104370675B discloses a process for producing polyalphaolefins in a continuous manner, and the method includes introducing alpha olefins into a continuous transparent microchannel reactor and carrying out a polymerization reaction in the presence of an aluminum compound catalyst and auxiliary agents to produce polyalphaolefins. This method consumes large amounts of catalyst and requires a higher reaction temperature.

In addition, the reaction process in the batch reactor reported in the prior art has the disadvantages of large mixing reactor volume, large occupied area, very stringent requirements for control of process parameters, complex process operation, long reaction time, long production period, etc., however, the continuous production method also cannot provide ideal conversion and selectivity, and in both methods the catalyst in the product cannot be well processed. Thus, there is a need in the art for a plant and process for producing alpha-olefin oligomers that are characterized by high conversion, high selectivity, ease of process, low capital investment, and safety and environmental friendliness.

It should be noted that the information disclosed in the preceding "Background Art" section is intended only to enhance the understanding of the prior art of the present invention and, therefore, may contain information that does not constitute prior art and is already known to one skilled in the art.

The essence of the invention

The present invention provides a plant and method for producing polyalphaolefins.

More specifically, the present invention includes the following aspects.

In a first aspect, the present invention provides a plant for the production of polyalphaolefins.

The plant for producing polyalphaolefins of the present invention includes an inlet unit 1, a microchannel reactor 2 and a post-processing unit 3, which are connected in series; the inlet assembly includes a mixer and/or pipeline(s) for supplying olefin feedstock, auxiliary feedstock and BF ₃ catalyst to microchannel reactor 2; inlet unit 1 contains at least a mixer for mixing at least part of the auxiliary raw material and at least part of the BF ₃ catalyst and a pipeline for separately supplying at least part of the BF ₃ catalyst into the microchannel reactor 2.

According to the installation of the present invention, the mixer in the inlet unit 1 may be a static and/or a dynamic mixer, preferably a static mixer, more preferably an enhanced mixing static mixer. Optionally, the mixer has the following structure and parameters: the operating temperature is from 20 to 200°C, and the upper limit of the operating pressure does not exceed 20 MPa. When two or more mixers are used, the mixers may be connected in parallel, in series, or in both parallel and series. The mixer may optionally have a heat transfer layer. The mixer may optionally contain filler; The filler in the mixer can be selected from Pall ring, ceramic ball, regular filler, corrugated filler, wire mesh or plastic ring.

In one embodiment of the present invention, in accordance with the installation of the present invention, the inlet assembly 1 may include a mixer for mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and a portion of the olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the remainder of the olefin feedstock, based on the feedstock type, into the microchannel reactor 2 (hereinafter also called setting mode 1).

In one embodiment of the present invention, in accordance with the installation of the present invention, optionally, the inlet assembly 1 includes a mixer for mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock, a conduit for separately passing the remainder of the BF ₃ catalyst into the microchannel reactor 2, and a conduit for separately passing all of the olefin feed material into microchannel reactor 2 (also called tuning mode 2 below).

In one embodiment of the present invention, in accordance with the apparatus of the present invention, optionally, the inlet assembly 1 includes a mixer for mixing a portion of the BF ₃ catalyst and a portion of the auxiliary feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the entire olefin feedstock. into microchannel reactor 2 (also called tuning mode 3 below).

In one embodiment of the present invention, in accordance with the installation of the present invention, optionally, the inlet assembly 1 includes a mixer for mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and the entire olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock into microchannel reactor 2 (also called tuning mode 4 below).

In one embodiment of the present invention, in accordance with the apparatus of the present invention, optionally, the inlet assembly 1 includes a mixer for mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and a portion of the olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst and the remainder of the olefin feedstock into microchannel reactor 2 (also called tuning mode 5 below).

In one embodiment of the present invention, in accordance with the installation of the present invention, optionally, the inlet assembly 1 includes a mixer for mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock and all of the olefin feedstock, and a conduit for separately passing the remainder of the BF ₃ catalyst into the microchannel reactor 2 (below also called setting mode 6).

In one embodiment of the present invention, in accordance with the installation of the present invention, it is preferable that the BF ₃ catalyst, auxiliary feedstock and olefin feedstock are mixed in the inlet unit 1 (i.e., the above-mentioned setting mode 1, setting mode 4, setting mode 5, mode settings 6), inlet assembly 1 includes a first mixer for mixing any two of the above three feedstocks and a second mixer for mixing a mixture of the first mixer and the remaining one feedstock, the first mixer being in communication with the second mixer and the second mixer being in communication with the microchannel reactor 2. More preferably, the inlet assembly 1 includes a first mixer for mixing one of the olefin feedstock and BF ₃ gas with the auxiliary feedstock, and a second mixer for subsequently mixing the mixture with the other olefin feedstock and BF ₃ gas. For example, the inlet unit 1 includes a first mixer for mixing the olefin feedstock with the auxiliary raw material and a second mixer for mixing the mixture with BF ₃ gas; or the inlet unit 1 comprises a first mixer for mixing the BF ₃ gas with the auxiliary feedstock and a second mixer for mixing the mixture with the olefin feedstock. The inlet unit 1 additionally contains pipelines that are in communication with the microchannel reactor 2, into which the remainder of each of the starting materials is fed separately.

In one embodiment of the present invention in accordance with the installation of the present invention, preferably the inlet assembly 1 includes a first mixer for mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock, a second mixer for mixing the stream obtained after mixing in the first mixer and all of the olefin feedstock, and a pipeline for separately passing the catalyst residue BF ₃ into the microchannel reactor 2. In addition, the first mixer is in communication with the second mixer, and the second mixer is in communication with the microchannel reactor 2.

In accordance with the installation of the present invention, the microchannel reactor 2 can provide a microchannel reaction of the mixed stream from the mixer in the inlet node and the streams from any separate pipelines in the inlet node. The number of microchannel reactors 2 can be one or more, preferably one, two, three, four, five or six. When using two or more microchannel reactors 2, these microchannel reactors 2 can be connected in series, in parallel, or both in parallel and in series.

The structure and parameters of microchannel reactor 2 are as follows: the reaction channel is 2-10000 parallel channels, the operating temperature range is from -70 to 300°C, the permissible maximum reaction pressure does not exceed 20 MPa, the permissible maximum pressure of the heat exchange medium does not exceed 10 MPa; the volume of the liquid channel without mixing inserts is 0.1-20000 l, the volumetric flow rate is 1-50000 l/h. Also preferably, the reaction channel is formed by 2-5000 channels, more preferably 2-500 channels. For example, a reaction channel may consist of 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22 channels, or etc. In the microchannel reactor of the present invention, each reaction channel may have a cross-sectional area from 1 to 150 mm ² and a length from 50 to 5000 mm. Preferably, each reaction channel is provided with a mixing element that promotes mixing of the reaction streams, and the mixing element is an element well known in the art that can promote mixing of the reaction streams and increase turbulence, and it can be a mixing disk as well as a first a mixing element and a second mixing element according to the present invention. Preferably, the microchannel reactor of the invention is provided with a main pipe for distributing the reaction gas and outlet pipes for distributing the reaction gas into each reaction channel.

In one embodiment of the present invention, in accordance with the apparatus of the present invention, the preferred microchannel reactor 2 (hereinafter sometimes also referred to as the preferred microchannel reactor of the present invention) includes:

building 003; a supply zone 023, a mixing zone 008, a reaction zone 009 and a collection zone 024 are arranged in series and are in communication along a first direction in the housing 003, and the housing 003 is provided with a supply pipe 002 in communication with the supply zone 023, and an outlet pipe 001 located in communication with the collection zone 024, and the mixing zone 008 is equipped with a mixing channel 014 running along the first direction;

pipe 017 for liquid distribution; a liquid distribution pipe 017 extends from the outside of the housing 003 into the mixing channel 014, the liquid distribution pipe 017 is connected to a liquid distributor 016 at the end of the mixing channel 014;

supply pipe 002 is used to introduce feedstock from inlet unit 1, liquid distribution pipe 017 is connected to the separately supplied BF ₃ catalyst pipeline of inlet unit 1 and can be used to introduce BF ₃ catalyst, and outlet pipe 001 is connected to high pressure separation unit 3.

In one embodiment of the present invention, there may be two or more supply pipes 002, the number of which corresponds to the pipes from the inlet unit 1, with the exception of the pipe for separately supplying the BF ₃ catalyst. These lines include a line for separate supply to the microchannel reactor (except for a separate supply of BF ₃ catalyst) and a line for connecting the last stage mixer to the microchannel reactor. In the present invention, the above-mentioned "last stage mixer" refers to a mixer in which the feedstock is mixed and which is then connected to the microchannel reactor through a pipeline in the inlet portion 1. In the present invention, the first direction is the flow direction, and this direction may be a horizontal direction , upward direction or the like. The upward direction is preferable, and the upward direction is more preferable.

In one embodiment of the present invention, the mixing zone 008 and the supply zone 023 may be separated by a first partition wall 019. The first partition wall 019 is provided with a plurality of through holes, and each through hole is aligned with the mixing channel 014, so that the mixing zone 008 is in communication with feed zone 023.

In one embodiment of the present invention in accordance with the installation of the present invention, preferably the supply pipe is connected to the mixer of the inlet assembly 1 to introduce a mixture of at least two components of at least a portion of the olefin feedstock, at least a portion of the auxiliary raw materials and at least part of the BF ₃ catalyst.

In one embodiment of the present invention, preferably the liquid distributor is at least one selected from a micropore powder sintered body, a mesoporous foam, a wire mesh, and a microslit or micropore tube. Preferably, the liquid distributor is a cylindrical powder sintered body with micropores.

In one embodiment of the present invention, preferably the liquid distributor has a cross-sectional area of 0.01-200 cm ² and a length of 1-2000 mm.

In one embodiment of the present invention, the mixing channel has a circular cross-section. The mixing channel has a cross-sectional area of 0.05-400 cm ² and a length of 50-5000 mm.

In the present invention, the length and cross-sectional area of the mixing channel 014 are both larger than the length and cross-sectional area of the liquid distributor 016.

In one embodiment of the present invention, the mixing zone is provided with 2-100 (preferably 2-50, more preferably 2-10) mixing channels, the liquid distribution pipe 017 includes a main pipe extending from the outside of the housing into the supply zone, and branch pipes extending from the supply zone to each mixing channel 014, with liquid distributors 016 connected to the ends of the outlet pipes.

In one embodiment of the present invention, in the mixing channel 014, the first mixing element 015 is located downstream of the liquid distributor 016.

In one embodiment of the present invention, the first mixing element 015 is provided with a main flow portion and a waste flow portion that are alternately arranged and in communication along the first direction, and the main flow portion is provided with one main flow passage and the waste flow portion is provided with a plurality of exhaust flow passages. Preferably, a collection cavity in communication with the plurality of bleed flow passages is located downstream of the bleed flow portion. The first mixing element may be formed by splicing a plurality of plate elements (the number may be 2-100, preferably 2-50, more preferably 10-30, thickness is approximately 0.2-10 mm) located along the first direction, and on each plate The element is formed with structures such as holes and cavities that correspond to the main flow passage 0001, the outlet flow passage 0002 and the collection cavity 0003, which is convenient for processing and production.

In one embodiment of the present invention, the mixing zone may include a first heat exchange cavity 013 located in the housing, wherein the mixing channel is located in the first heat exchange cavity, and the housing is provided with a first heat exchange medium inlet 004 and a first heat exchange medium outlet 005, which are in communication with the first heat exchange cavity.

In one embodiment of the present invention, the volumetric ratio of the first heat exchange cavity to the mixing channel is 2-50; preferably the volume ratio of the first heat exchange cavity to the mixing channel is 5-30. In the mixing zone 008, the mixing channel 014 and the first heat exchange cavity 013 are isolated from each other and are not in communication with each other, but heat transfer between them can be ensured, and pipe fittings with good thermal conductivity can be used in the mixing channel 014.

In one embodiment of the present invention, a transition zone 020 is provided between the mixing zone and the reaction zone, wherein the transition zone is provided with a stabilizing channel 021 of constant cross-section and a diffusion channel 022 of gradually increasing cross-section, which are located and in communication along the first direction, the stabilizing the channel is in communication with the mixing channel, and the diffusion channel is in communication with the reaction zone.

In one embodiment of the present invention, the outlet pipe 018 extending to the outside of the housing is connected to the stabilizing channel.

In one embodiment of the present invention, the diffusion channel is provided with a diffusion plate with cells or slits.

In one embodiment of the present invention, the two ends of the transition zone 020 are respectively provided with partition walls with through holes so that they are isolated from the mixing zone 008 (mainly the first heat exchange cavity 013) and the reaction zone 009 (mainly the second heat exchange cavity 012) and connected to each mixing channel 014 and each reaction channel 010 through each through hole on each partition wall, and the diffusion channel 022 and the stabilizing channel 021 may be pipe fittings provided between the two partition walls.

In one embodiment of the present invention, the reaction zone is provided with a plurality of parallel reaction channels extending along a first direction and in communication with the mixing channel through a stabilizing channel 021 and a diffusion channel 022. The reaction channel has a cross-section of at least one of circular, rectangular and triangular shapes. The number of reaction channels is, for example, 2-10000 channels, preferably 2-5000 channels, and more preferably 2-500 channels.

In one embodiment of the present invention, the reaction channel is provided with a second mixing element, and the second mixing element includes a support bar extending along the first direction, and a toothed element connected to the support bar and extending across the support bar; the toothed element has at least one of triangular, arcuate, wavy and spiral shapes. Preferably, the gear element has a triangular shape, and on one side of the triangle adjacent to the support bar, one corner is connected to the support bar and the other corner is spaced from the support bar by 0.01-20 mm.

In one embodiment of the present invention, each of the reaction channels is independently provided with a plurality of second mixing elements (the number may be 2-100, preferably 2-50, more preferably 10-30), which are stacked on top of each other at intervals, and the toothed elements of the second mixing element are staggered relative to each other.

Preferably, the cross-section of the reaction channel is rectangular and the toothed elements extend between a set of opposite sides of the rectangle.

In one embodiment of the present invention, the reaction channel has a cross-sectional area of 1-150 mm ² and a length of 50-5000 mm, the minimum distance between the reaction channels is 1-50 mm, and the second mixing element has a thickness of 0.1-3 mm, wherein the distance between adjacent gear elements is 1-50 mm; preferably the reaction channel has a length of 100-3000 mm and the minimum gap between the reaction channels is 3-30 mm, the second mixing element has a thickness of 0.2-2 mm, and the gap between adjacent toothed elements is 1.5-20 mm.

In one embodiment of the present invention, the reaction zone may be provided with a second heat exchange cavity 012 located in the housing, wherein the reaction channel is located in the second heat exchange cavity, the housing is provided with a second heat exchange medium inlet 006 and a second heat exchange medium outlet 007, which are in communication with second heat exchange cavity.

In one embodiment of the present invention, the volumetric ratio of the second heat exchange cavity to the reaction channel is 2-50; preferably the volumetric ratio of the second heat exchange cavity to the reaction channel is 5-30.

In one embodiment of the present invention, the second heat exchange cavity 012 may advantageously be formed by the housing 003, and at the two ends, respectively, there are a second dividing wall 025 between the reaction zone 009 and the collection zone 024 and a dividing wall between the reaction zone 009 and the transition zone 020.

In accordance with the installation of the present invention, the post-processing unit 3 provides post-processing of the incoming stream to obtain a polyolefin product. The post-processing unit 3 may be one or more of an adsorption device, a centrifugation device, a sedimentation device, an alkali washing device, an aqueous washing device, and a gas-liquid separation device.

In one embodiment of the present invention, in accordance with the installation of the present invention in the adsorption device, the catalyst in the stream is removed after adsorption by the adsorbent in the adsorption device to obtain a crude polyolefin product, which can be further subjected to subsequent processing to obtain a final polyolefin product. The adsorbent may be one or more of a metal oxide, an ion exchange resin, and an activated bleach earth. The metal oxide is preferably one or more of potassium oxide, calcium oxide, sodium oxide, magnesium oxide, alumina and barium oxide. The adsorption device may be one or more of a fluidized bed, a fixed bed, and a continuous mixing vessel.

In one embodiment of the present invention, in accordance with the installation of the present invention, the sedimentation device or the centrifugation device causes the stream obtained after the polymerization reaction to be separated into a light liquid phase and a heavy liquid phase. The light liquid phase represents the crude polyolefin product and can be subjected to further downstream processing to produce the final polyolefin product; the heavy liquid phase contains the auxiliary feedstock complex and BF ₃ and unreacted olefin feedstock and can be returned to the inlet assembly or microchannel reactor for reuse. Further, the centrifugation device is preferably a centrifuge, which may be one or more of a conical plate centrifuge, a tube centrifuge and a horizontal centrifuge.

In one embodiment of the present invention, in accordance with the installation of the present invention, the alkaline washing device can pass the stream obtained from the polymerization reaction into an alkaline aqueous solution to remove the catalyst, and the resulting stream is then subjected to aqueous washing, liquid-liquid separation and drying to obtain the final polyolefin product.

In one embodiment of the present invention, in accordance with the installation of the present invention, the aqueous washing device can pass the stream obtained from the polymerization reaction into water to remove the catalyst by washing with water, and the resulting stream is then subjected to liquid-liquid separation and drying to obtain the final polyolefin product .

In one embodiment of the present invention, in accordance with the installation of the present invention, the gas-liquid separation device can remove catalyst from the stream obtained from the polymerization reaction by gas-liquid separation, and the final liquid phase obtained after gas-liquid separation is then subjected to subsequent processing to obtain the final polyolefin product. The gas phase obtained after gas-liquid separation (BF ₃ gas) can be recycled for use.

In accordance with the installation of the present invention, based on the total mass of BF ₃ in the microchannel reactor 2, the mass ratio of the BF ₃ catalyst directly supplied to the microchannel reactor 2 to the BF ₃ catalyst mixed in the mixer of the inlet unit 1 is 90-10:10- 90, preferably 80-40:20-60, more preferably 70-50:30-50.

In the present invention, the total mass of BF ₃ in the microchannel reactor 2 refers to the total mass of BF ₃ complexed with the auxiliary feedstock and free BF ₃ in the microchannel reactor 2. In other words, it represents the total mass of BF ₃ in the feed stream from the mixer of the last stage of inlet unit 1 into the microchannel reactor (total mass of BF ₃ in the complex and free BF ₃ in the stream), and the mass of BF ₃ catalyst separately supplied to the microchannel reactor. That is, it represents the total mass of BF ₃ supplied to the inlet unit 1, and BF ₃ separately supplied to the microchannel reactor 2. In the present invention, the BF ₃ catalyst refers to free BF ₃ , which does not form a complex with the auxiliary raw material, also known as BF ₃ -gas or BF ₃ .

The polyalphaolefin production apparatus of the present invention can be used to synthesize polyalphaolefin synthetic oil. The apparatus of the invention can realize flexible and rapid mixing of catalyst, auxiliary raw materials and olefin starting material, and has the advantages of high polymerization reaction speed, good mass transfer and heat transfer effects, high reaction conversion, good product selectivity and excellent productivity, making it suitable for large-scale industrial production. production.

The polyalphaolefin production apparatus using the preferred microchannel reactor in the present invention can continuously and efficiently mix the reaction system, maintain liquid flow in a piston-like mode and stir, ensure that the residence time of the reaction liquid is constant as much as possible, and also avoid selectivity for undesirable products due to residence time distribution.

In a second aspect, the present invention provides a method for producing polyalphaolefins.

The method for producing polyalphaolefins of the present invention includes: BF ₃ catalyst, auxiliary raw materials and olefin starting material are passed into a microchannel reactor through an inlet unit and subjected to a polymerization reaction in the microchannel reactor, and then further processed to obtain a polyolefin product, wherein at the inlet unit they are mixed with at least at least part of the auxiliary raw material and at least part of the BF ₃ catalyst and at the same time at least part of the BF ₃ catalyst are separately fed into the microchannel reactor.

According to the method of the invention, preferably at least a portion of the olefin feedstock, at least a portion of the auxiliary feedstock, and at least a portion of the BF ₃ catalyst are mixed in the inlet assembly.

In one embodiment of the present invention, the olefin in the olefin feedstock is one or more C ₃ -C ₂₀ alpha olefins, preferably one or more C ₅ -C ₁₅ alpha olefins, more preferably one or more C ₇ -C ₁₄ -alpha-olefins. For example, the olefin may be olefins commonly used in the production of PAO synthetic base oils, such as nonene and decene.

In one embodiment of the present invention, the olefin feedstock may also contain a C ₅ -C ₂₀ alkane and/or a C ₁ -C ₂₀ oxygen-containing compound as a solvent. Relative to the total weight of the olefin feedstock, the mass fraction of C ₅ -C ₂₀ alkane may be 0-80%, preferably 0.5-50%, most preferably 1-30%. Relative to the total weight of the olefin starting material, the mass fraction of the C ₁ -C ₂₀ oxygen-containing compound may be 0-20%, preferably 0-10%, most preferably 0.001-5%. The C ₅ -C ₂₀ -alkane may be one or more of n-alkane, isoalkane and cycloalkane; The C ₁ -C ₂₀ oxygen-containing compound may be one or more of an n-alkanol, an isoalcohol, and a ketone. The Fischer-Tropsch olefin feedstock can be used as a mixture of a C ₃ -C ₂₀ alpha-olefin, a C ₅ -C ₂₀ alkane and a C ₁ -C ₂₀ oxygen-containing compound (ie, as an olefin feedstock).

In one embodiment of the present invention, the auxiliary raw material may be a commonly used auxiliary raw material that can be used as a BF ₃ electron donor, and may be one or more of an alcohol having a carbon number of 1-20, an ether, having a number of carbon atoms of 1-20, an aldehyde having a number of carbon atoms of 1-20, a ketone having a number of carbon atoms of 1-20, an ester having a number of carbon atoms of 1-30, a carboxylic acid having a number of carbon atoms of 1-20, and a phenol having a carbon number of 1 to 20, preferably from an alcohol having a carbon number of 1 to 10, more preferably an alcohol having a carbon number of 3 to 5, for example from one or more of n-propanol, isopropanol, n-butanol, isobutanol, n-pentanol and isopentanol.

In one embodiment of the present invention in accordance with the method of the invention, preferably in a microchannel reactor the mass ratio of (auxiliary feedstock):(olefin feed):(total BF ₃ catalyst) is 1:1-1000:1-500 (preferably 1:1 -500:1-200, most preferably 1:10-250:1-100). The mass ratio (auxiliary feedstock):(olefin feedstock):(whole BF ₃ catalyst) refers to the mass ratio of the feedstocks when all the feedstocks are fed into the microchannel reactor, that is, it may represent the proportion, based on individual calculation, of the feedstocks reaction materials in the stream immediately downstream of the liquid distributor. In the present invention, the mass of the auxiliary raw material includes the mass of the auxiliary agent in the BF ₃ complex, and the mass of BF ₃ includes the mass of BF ₃ in the BF ₃ complex.

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and a portion of the olefin feedstock may be mixed and passed into the microchannel reactor, and the remaining BF ₃ catalyst, the remaining auxiliary feedstock, and the remaining olefin feedstock The material, based on the type of feedstock, is each separately passed into the microchannel reactor (hereinafter also called feed mode 1).

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, the stream obtained by mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock may be passed into a microchannel reactor, and each of the remainder of the BF ₃ catalyst and the entire olefin feedstock is separately passed into microchannel reactor (hereinafter also called feed mode 2). Preferably, in the case of mixing part of the BF ₃ catalyst and all the auxiliary raw materials in the mixer, the flow rate of part of the BF ₃ catalyst into the mixer is 1-100,000 l/h, preferably 1-80,000 l/h, most preferably 1-30,000 l/h; the flow rate of all auxiliary raw materials into the mixer is 0.01-1000 l/hour, preferably 0.1-800 l/hour, most preferably 0.2-500 l/hour; the flow rate of the mixture obtained after mixing part of the BF ₃ catalyst and all the auxiliary raw materials in the mixer into the microchannel reactor is 0.01-2000 l/h, preferably 0.1-1600 l/h, most preferably 0.2-1000 l/h hour; the individual flow rate of the remaining BF ₃ catalyst into the microchannel reactor is 1-150,000 L/hour, preferably 5-100,000 L/hour, most preferably 10-50,000 L/hour, the individual flow rate of all olefin feed material into the microchannel reactor is 10-5000 L /hour, preferably 20-4000 l/hour, most preferably 40-2500 l/hour.

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, the stream obtained by mixing a portion of the BF ₃ catalyst and a portion of the auxiliary feedstock may be passed into a microchannel reactor, and each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the total olefin the starting material is separately passed into the microchannel reactor (hereinafter also called feed mode 3). Preferably, in the case of mixing part of the BF ₃ catalyst and part of the auxiliary raw material in the mixer, the flow rate of part of the BF ₃ catalyst into the mixer is 1-100,000 l/h, preferably 1-80,000 l/h, most preferably 1-30,000 l/h; the flow rate of part of the auxiliary raw material into the mixer is 0.01-800 l/hour, preferably 0.1-500 l/hour, most preferably 0.2-400 l/hour; the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst and part of the auxiliary raw material in the mixer into the microchannel reactor is 0.01-1600 l/h, preferably 0.1-1400 l/h, most preferably 0.2-800 l/h hour; the rate at which the remaining BF ₃ catalyst passes separately into the microchannel reactor is 1-120,000 l/h, preferably 5-80,000 l/h, most preferably 10-40,000 l/h; the flow rate of the remainder of the auxiliary raw material into the mixer is 0.01-200 l/hour, preferably 0.1-150 l/hour, most preferably 0.2-100 l/hour; the individual flow rate of all olefin feedstock into the microchannel reactor is 10-5000 L/hour, preferably 20-4000 L/hour, most preferably 40-2500 L/hour).

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, the stream obtained by mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and all of the olefin feedstock may be passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder auxiliary raw materials are individually passed into the microchannel reactor (hereinafter also called feed mode 4). Preferably, when mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and all of the olefin feedstock in a mixer, the flow rate of the portion of the BF ₃ catalyst into the mixer is 1-100,000 L/hr, preferably 1-80,000 L/hr, most preferably 1-30,000 L/hr. hour; the flow rate of part of the auxiliary raw material into the mixer is 0.01-800 l/hour, preferably 0.1-500 l/hour, most preferably 0.2-400 l/hour; the flow rate of the total olefin feed into the mixer is 10-5000 L/hour, preferably 20-4000 L/hour, most preferably 40-2500 L/hour; the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst, part of the auxiliary raw material and all of the olefin feedstock in the mixer into the microchannel reactor is 0.01-6000 l/h, preferably 0.1-4600 l/h, most preferably 0. 2-3000 l/hour; the rate at which the remaining BF ₃ catalyst passes separately into the microchannel reactor is 1-150,000 l/h, preferably 5-100,000 l/h, most preferably 10-50,000 l/h; the rate at which the remainder of the auxiliary raw material is passed separately into the microchannel reactor is 0.01-200 l/hour, preferably 0.1-150 l/hour, most preferably 0.2-100 l/hour).

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, the stream obtained by mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and a portion of the olefin feedstock may be passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder The olefin feedstock is separately passed into the microchannel reactor (hereinafter also referred to as feed mode 5). Preferably, in the case of mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock and a portion of the olefin feedstock in a mixer, the flow rate of the portion of the BF ₃ catalyst into the mixer is 1-100,000 L/hour, preferably 1-80,000 L/hour, most preferably 1-30,000 L /hour; the flow rate of all auxiliary raw materials into the mixer is 0.01-1000 l/hour, preferably 0.1-800 l/hour, most preferably 0.2-500 l/hour; the flow rate of a portion of the olefin feedstock into the mixer is 1-2000 L/hour, preferably 5-1000 L/hour, most preferably 10-500 L/hour; the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst, all of the auxiliary raw materials and part of the olefin feedstock in the mixer into the microchannel reactor is 0.01-3000 l/h, preferably 0.1-1800 l/h, most preferably 0. 2-1000 l/hour; the rate at which the BF ₃ catalyst residue passes separately into the microchannel reactor is 1-150,000 l/h, preferably 5-100,000 l/h, most preferably 10-50,000 l/h; the rate of passing separately the remainder of the olefin feed into the microchannel reactor is 9-3000 l/h, preferably 15-3000 l/h, most preferably 30-2000 l/h).

In one embodiment of the present invention, in accordance with the method of the invention, at the inlet assembly, the stream obtained by mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and all of the olefin feedstock may be passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor (hereinafter also called feed mode 6). Preferably, in the case of mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and all of the olefin feedstock in a mixer, the flow rate of the portion of the BF ₃ catalyst into the mixer is 1-100,000 L/hr, preferably 1-80,000 L/hr, most preferably 1-30,000 L /hour; the flow rate of all auxiliary raw materials into the mixer is 0.01-1000 l/h, preferably 0.1-800 l/h, most preferably 0.2-500 l/h; the flow rate of the total olefin feed into the mixer is 10-5000 L/hour, preferably 20-4000 L/hour, most preferably 40-2500 L/hour; the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst, all of the auxiliary raw materials and all of the olefin feedstock in the mixer into the microchannel reactor is 10-6000 l/h, preferably 0.1-4600 l/h, most preferably 0.2- 3000 l/hour; the rate at which the BF ₃ catalyst residue passes separately into the microchannel reactor is 1-150,000 l/h, preferably 5-100,000 l/h, most preferably 10-50,000 l/h).

In one embodiment of the present invention, in accordance with the method of the invention, preferably at the inlet assembly, a portion of the BF ₃ catalyst and all auxiliary feedstocks may be subjected to a first mixing in a first mixer, then the stream resulting from the first mixing is subjected to a second mixing with all of the olefin feedstock, and the stream obtained after the second mixing is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor; Preferably, when the BF ₃ catalyst portion and all auxiliary raw materials are subjected to first mixing in the first mixer, the flow rate of the BF ₃ catalyst portion into the first mixer is 1-100,000 l/h, preferably 1-80,000 l/h, most preferably 1-30,000 l/h hour; the flow rate of all auxiliary raw materials into the first mixer is 0.01-1000 l/hour, preferably 0.1-800 l/hour, most preferably 0.2-500 l/hour; the stream obtained from the first mixing is then subjected to a second mixing with all the olefin feed material in a second mixer, and the flow rate of the stream obtained from the first mixing into the second mixer is 0.01-2000 l/hour, preferably 0.1-1600 l /hour, most preferably 0.2-1000 l/hour; the flow rate of the total olefin feed into the second mixer is 10-5000 L/hour, preferably 20-4000 L/hour, most preferably 40-2500 L/hour; the flow rate of the flow obtained after the second mixing into the microchannel reactor is 10-7000 l/h, preferably 20-5600 l/h, most preferably 40-3500 l/h; the rate of passage of the BF ₃ catalyst residue separately into the microchannel reactor is 1-150,000 l/h, preferably 5-100,000 l/h, most preferably 10-50,000 l/h.

In one embodiment of the present invention, in accordance with the method of the invention, preferably the reaction temperature in the microchannel reactor is 0-120°C, preferably 10-80°C, more preferably 20-60°C. According to the method of the invention, preferably the reaction pressure in the microchannel reactor is 0.01-10 MPa, preferably 0.01-8 MPa, more preferably 0.1-6 MPa. According to the method of the invention, preferably the residence time of the olefin feedstock in the microchannel reactor is 1-3600 seconds, preferably 10-1800 seconds, more preferably 15-1000 seconds.

According to the method of the present invention, any of the microchannel reactors described in the first aspect can be used as the microchannel reactor.

In one embodiment of the present invention, according to the method of the invention, preferably the post-treatment method is one or more of adsorption, centrifugation, precipitation, alkaline washing, aqueous washing and gas-liquid separation methods, preferably an adsorption method. The adsorbent in the adsorption method is preferably one or more of a metal oxide, an ion exchange resin, activated bleaching earth and a molecular sieve, more preferably a metal oxide, and the metal oxide is preferably one or more of potassium oxide, calcium oxide, sodium oxide, magnesium oxide, aluminum oxide and barium oxide.

In one embodiment of the present invention, in accordance with the method of the invention, preferably when the after-treatment method is sedimentation or centrifugation, the sedimentation or centrifugation causes the stream entering the after-treatment unit to be separated into a light liquid phase and a heavy liquid phase. The heavy liquid phase contains a complex of auxiliary feedstocks and BF ₃ and unreacted olefin feedstock, and is optionally returned to the inlet assembly or microchannel reactor to continue to participate in the continuous reaction. The light liquid phase represents the crude polyolefin product and can be subject to further downstream processing.

In accordance with the method of the present invention, preferably the resulting polyolefin product is subjected to fractionation, hydrogenation and optional blending steps to produce a synthetic oil that is viscosity grade appropriate.

The method of the present invention has the advantages of high polymerization speed, good mass transfer and heat transfer effects, high reaction conversion, good product selectivity and good productivity, and is suitable for large-scale industrial production.

In a third aspect, the present invention provides a method for producing polyalphaolefins using any of the plants described in the first aspect.

A method for producing polyalphaolefins using any of the plants for producing polyalphaolefins described in the first aspect in accordance with the invention includes: BF ₃ catalyst, auxiliary raw materials and olefin starting material are passed into the microchannel reactor through the inlet unit 1 and subjected to a polymerization reaction in the microchannel reactor, and then subsequent processing to obtain a polyolefin product, where in the inlet unit 1 at least part of the auxiliary raw material and at least part of the BF ₃ catalyst are mixed and at the same time at least part of the BF ₃ catalyst is separately fed into the microchannel reactor 2.

In one embodiment of the present invention, the olefin in the olefin feedstock is one or more C ₃ -C ₂₀ alpha olefins, preferably one or more C ₅ -C ₁₅ alpha olefins, more preferably one or more from among C ₇ -C ₁₄ alpha-olefins. For example, the olefin may be olefins commonly used in the production of PAO synthetic base oils, such as nonene and decene.

In one embodiment of the invention, the olefin feedstock may also contain a C ₅ -C ₂₀ alkane and/or a C ₁ -C ₂₀ oxygen-containing compound as a solvent. Relative to the total weight of the olefin feedstock, the mass fraction of C ₅ -C ₂₀ alkane may be 0-80%, preferably 0.5-50%, most preferably 1-30%. Relative to the total weight of the olefin feedstock, the mass fraction of the C ₁ -C ₂₀ oxygen-containing compound may be 0-20%, preferably 0-10%, most preferably 0.001-5%. The C ₅ -C ₂₀ -alkane may be one or more of n-alkane, isoalkane and cycloalkane; The C ₁ -C ₂₀ oxygen-containing compound may be one or more of an n-alkanol, an isoalcohol, and a ketone. The Fischer-Tropsch olefin feedstock can be used as a mixture of a C ₃ -C ₂₀ alpha-olefin, a C ₅ -C ₂₀ alkane and a C ₁ -C ₂₀ oxygen-containing compound (ie, as an olefin feedstock).

In one embodiment of the invention, the auxiliary raw material may be a commonly used auxiliary raw material that can be used as a BF ₃ electron donor, and may be one or more of an alcohol having 1-20 carbon atoms, an ether having a number of carbon atoms of 1-20, an aldehyde having a number of carbon atoms of 1-20, a ketone having a number of carbon atoms of 1-20, an ester having a number of carbon atoms of 1-30, a carboxylic acid having a number of carbon atoms of 1-20, and phenol having 1-20 carbon atoms, preferably from an alcohol having 1-10 carbon atoms, more preferably an alcohol having 3-5 carbon atoms, for example one or more of n-propanol, isopropanol, n- butanol, isobutanol, n-pentanol and isopentanol.

In one embodiment of the present invention in accordance with the method of the invention, preferably in a microchannel reactor the mass ratio of (auxiliary feedstock):(olefin feed):(total BF ₃ catalyst) is 1:1-1000:1-500 (preferably 1:1 -500:1-200, most preferably 1:10-250:1-100). The mass ratio (auxiliary feedstock):(olefin feedstock):(whole BF ₃ catalyst) refers to the mass ratio of the feedstocks when all the feedstocks are fed into the microchannel reactor, that is, it may represent the proportion, based on individual calculation, of the feedstocks reaction materials in the stream immediately downstream of the liquid distributor. In the present invention, the mass of the auxiliary raw material includes the mass of the auxiliary agent in the BF ₃ complex, and the mass of BF ₃ includes the mass of BF ₃ in the BF ₃ complex.

In one embodiment of the present invention, according to the method of the invention, preferably the reaction temperature in the microchannel reactor 2 is 0-120°C, preferably 10-80°C, more preferably 20-60°C. According to the method of the invention, preferably the reaction pressure in the microchannel reactor 2 is 0.01-10 MPa, preferably 0.01-8 MPa, more preferably 0.1-6 MPa. According to the method of the present invention, preferably the residence time of the olefin feedstock in the microchannel reactor 2 is 1-3600 seconds, preferably 10-1800 seconds, more preferably 15-1000 seconds.

In one embodiment of the present invention in accordance with the method of the invention, based on the total mass of BF ₃ in the microchannel reactor, the mass ratio of the BF ₃ catalyst directly fed into the microchannel reactor 2 to the BF ₃ catalyst involved in mixing in the inlet unit 1 is, is 90-10:10-90, preferably 80-40:20-60, more preferably 70-50:30-50.

In one embodiment of the present invention, in accordance with the method of the invention, preferably the post-treatment method is one or more of adsorption, centrifugation, precipitation, alkaline washing, aqueous washing and gas-liquid separation methods, preferably an adsorption method. The adsorbent in the absorption method is preferably one or more of a metal oxide, an ion exchange resin, activated bleaching earth and a molecular sieve, more preferably is a metal oxide, and the metal oxide is preferably one or more of potassium oxide, calcium oxide, sodium oxide , magnesium oxide, aluminum oxide and barium oxide.

In one embodiment of the present invention, in accordance with the method of the invention, preferably when the after-treatment method is sedimentation or centrifugation, the sedimentation or centrifugation causes the stream entering the after-treatment unit to be separated into a light liquid phase and a heavy liquid phase. The heavy liquid phase contains the auxiliary feedstock and BF ₃ complex and unreacted olefin feedstock and is optionally returned to the inlet or microchannel reactor to continue to participate in the continuous reaction. The light liquid phase represents the crude polyolefin product and can be subject to further downstream processing.

According to the method of the invention, the resulting polyolefin product is preferably subjected to fractionation, hydrogenation and optional blending operations to obtain a synthetic oil that is viscosity grade appropriate.

The method of the present invention can realize flexible and rapid mixing of catalyst, auxiliary raw material and olefin starting material, and has the advantages of high polymerization reaction speed, good mass transfer and heat transfer effects, high reaction conversion, good product selectivity and excellent productivity, making it suitable for large-scale production. industrial production.

The process for producing polyalphaolefins using the preferred microchannel reactor of the present invention can achieve continuous and efficient mixing of the reaction system, maintain liquid flow in a piston-like mode, ensure that the residence time of the reaction liquid is as constant as possible, and avoid selectivity to undesirable products due to for distribution of residence time.

Brief description of drawings

FIG. 1 is a schematic diagram of an apparatus according to the present invention.

FIG. 2 is a schematic diagram of an apparatus according to the present invention.

FIG. 3 is a schematic diagram of a preferred microchannel reactor of the present invention.

FIG. 4 is a cross-sectional view of a first mixing element in accordance with the present invention.

FIG. 5 shows a structural representation of a second mixing element in accordance with the present invention.

FIG. 6 shows a structural representation for stacking a plurality of second mixing elements in accordance with the present invention.

FIG. 7 is a schematic diagram of a comparative installation according to the present invention.

Description of item numbers

1: Inlet assembly

2: Microchannel reactor

3: Post-processing unit

01: BF ₃ catalytic converter inlet

02: Auxiliary raw material inlet

03: Olefin feedstock inlet

001: Exhaust pipe

002: Supply pipe

003: Housing

004: First heat exchange medium inlet

005: First outlet of heat exchange medium

006: Second heat exchange medium inlet

007: Second outlet of heat exchange medium

008: Mixing zone

009: Reaction zone

010: Reaction channel

011: Second mixing element

012: Second heat exchange cavity

013: First heat exchange cavity

014: Mixing channel

015: First mixing element

016: Fluid distributor

017: Liquid distribution pipe

018: Exhaust pipe

019: First dividing wall

020: Transition Zone

021: Stabilizing channel

022: Diffusion channel

023: Feed area

024: Collection area

025: Second dividing wall

0001: Main stream pass

0002: Diversion flow passage

0003: Collection cavity

0004: Support bar

0005: Toothed element.

Detailed description

The present invention is described below further by way of examples and in conjunction with the accompanying drawings.

FIG. 1 is a schematic diagram of a plant for producing polyalphaolefins according to the present invention, the plant including an inlet unit 1, a microchannel reactor 2 and a post-processing unit 3, which are connected in series, wherein the inlet unit 1 includes a mixer 11 for mixing BF ₃ catalyst and auxiliary raw materials, a mixer 12 for mixing a mixture of BF ₃ catalyst and auxiliary raw materials and an olefin feedstock, conduits for separately introducing the BF ₃ catalyst and an olefin feedstock, one tap of the mixer 11 may be in communication with the mixer 12, and another tap of the mixer 11 may be in communication with microchannel reactor 2, and mixer 12 is in communication with mixer 12.

FIG. 2 is a schematic diagram of a plant for producing polyalphaolefins according to the invention, the plant including an inlet unit 1, a microchannel reactor 2 and a post-processing unit 3, which are connected in series, wherein the inlet unit 1 includes a mixer 11 for mixing BF ₃ catalyst and auxiliary raw materials, a mixer 12 for mixing a mixture of BF ₃ catalyst and auxiliary raw materials and olefin feedstock, a pipeline for separately introducing BF ₃ catalyst, where the mixer 11 is in communication with the mixer 12, and the mixer 12 is in communication with the microchannel reactor 2.

FIG. 3 is a schematic representation of a preferred microchannel reactor of the present invention, which includes:

building 003; a supply zone 023, a mixing zone 008, a reaction zone 009 and a collection zone 024 are arranged in series and are in communication along a first direction in the housing 003, and the housing 003 is provided with a supply pipe 002 in communication with the supply zone 023, and an outlet pipe 001 located in communication with the collection zone 024, and the mixing zone 008 is equipped with a mixing channel 014 running along the first direction;

pipe 017 for liquid distribution; a liquid distribution pipe 017 extends from the outside of the housing 003 into the mixing channel 014, the liquid distribution pipe 017 is connected to a liquid distributor 016 at the end of the mixing channel 014.

The housing 003 is the main container for housing the reactant and product, and the supply zone 023, the mixing zone 008, the reaction zone 009 and the collection zone 024 are different zones of the interior of the housing 003 (all of which can accommodate flow), and these zones are located in a straight line line so that the reactant (and product) moves in a straight line. In the present invention, the flow direction of the flow is called the first direction. Preferably, as shown in FIG. 3, the housing 003 is positioned such that the first direction is an upward direction, and the feeding zone 023, mixing zone 008, reaction zone 009 and collection zone 024 are arranged in the bottom-up direction.

The first group of reaction stream (the mixed stream from the inlet node 1, where there may be two or more feed pipes 002, the number of which corresponds to the number of pipelines from the inlet node 1, excluding the pipeline for separate supply of catalyst BF ₃ ) can be supplied to the feed zone 023 through feed pipe 002 on the body 003, and the feed zone 023 has a relatively large cavity and can act as a storage for the first group of reaction stream, wherein the first group of reaction stream in the supply zone 023 can flow into the adjacent mixing zone 008, that is, into the mixing channel 014. The liquid distribution pipe 017 is connected to the BF ₃ catalyst separate supply pipe in the inlet portion 1, therefore, the introduction of the second group of reaction stream (the separately supplied BF ₃ catalyst) can be conducted into the mixing channel 014 through the liquid distribution pipe 017 to ensure mixing the first reaction stream group and the second reaction stream group with each other in the mixing channel 014 of the mixing zone 008. In addition, the outlet end of the liquid distribution pipe 017 is provided with a liquid distributor 016. The liquid distributor 016 can convert the second reaction flow group into smaller droplets or bubbles, so that the second reaction flow group can be more evenly distributed in the first reaction flow group in the mixing channel 014. Moreover, the mixing structure in the mixing channel 014 is more acceptable for mixing liquid-phase flow and gas-phase flow. The first group of reaction stream is a liquid phase stream, and the second group of reaction stream is a gas phase stream. The gas-phase flow can be formed into dispersed microbubbles by the liquid distributor 016 to increase the contact area with the liquid-phase flow, and at the same time can also influence the liquid-phase flow to a greater extent, thereby improving the mixing uniformity of the two flows.

In addition, as shown in FIG. 3, the mixing channel 014 is a cavity extending along the first direction, that is, the mixing channel 014 has a substantially tubular structure, thereby allowing flow therein to flow along the first direction to form a stable piston flow.

The preferred microchannel reactor provided by the present invention, by designing the structure of the mixing channel and the mixing mode therein, can achieve continuous and efficient mixing of the reaction stream, and at the same time can maintain the flow of the reaction liquid in a piston flow mode, ensure that the residence time of the reaction liquid is constant as much as possible, and avoid selectivity for undesirable products due to residence time distribution.

More specifically, the liquid distributor 016 is at least one selected from a micropore powder sintered body, a mesoporous foam, a wire mesh, a microslit tube, or a micropore tube. The micro-pore powder sintered body can be produced by sintering the powder into a micro-pore structure through a powder metallurgy process, the hollow/mesoporous foam is a hollow micro-channel with mesh frames, the wire mesh is a micro-pore mesh structure, and the tube is provided with micro-slits or micro-holes which all can disperse liquid from pipe 017 to distribute liquid into smaller bubbles or droplets.

Preferably, the liquid distributor 016 is a cylindrical powder sintered body with micropores, and the mixing channel 014 has a circular cross-section. The liquid distributor 016 may be a structure having substantially the same outer diameter as the liquid distribution pipe 017, the cross-sectional shape of the liquid distributor 016 substantially matches the cross-sectional shape of the mixing channel 014, and the liquid distributor 016 may be positioned coaxially with the mixing channel 014 to allow the liquid flow dispersed by the liquid distributor 016 to mix more evenly with the flow in the mixing channel 014 and form a stable and uniform piston flow to eliminate inconsistency in the residence time of the flow.

In addition, the liquid distributor 016 has a cross-sectional area of 0.01-200 cm ² and a length of 1-2000 mm. Mixing channel 014 has a cross-sectional area of 0.05-400 cm ² and a length of 50-5000 mm. The length and cross-sectional area of the mixing channel 014 are both greater than the length and cross-sectional area of the liquid distributor 016.

In addition, the mixing zone 008 is provided with 2-100 (preferably 2-50, more preferably 2-10) mixing channels 014, the liquid distribution pipe 017 includes a main pipe extending from the outside of the housing 003 to the supply zone 023, and branch pipes, passing from the supply zone 023 into each mixing channel 014 with liquid distributors 016 connected to the ends of the outlet pipes. A plurality of mixing channels 014 are respectively in communication with the supply zone 023, and the first reaction stream group is divided into a plurality of portions in the mixing channels, which play a role in dispersing the first reaction stream group and allowing the first reaction stream group to form a stable, uniform piston flow. The liquid distribution pipe 017 includes a main pipe and branch pipes, wherein the main pipe is connected to the catalyst separate supply line BF ₃ in the inlet portion 1 and extends from the position of the housing 003 corresponding to the supply zone 023 to the supply zone 023, and the branch pipes extend from supply zones 023 to the mixing channels 014. That is, a liquid distribution pipe 017 extends from the supply zone 023 to the mixing channels 014. The mixing zone 008 and the supply zone 023 may be separated by a first partition wall 019. The first partition wall 019 is provided with a plurality of through holes, and each mixing channel 014 is aligned with each through hole, so that the mixing zone 008 is in communication with the supply zone 023.

In addition, in the mixing channel 014, the first mixing element 015 is located downstream of the liquid distributor 016. In the mixing channel 014, the downstream position of the liquid distributor 016 refers to a position downstream in the direction of liquid flow (that is, downstream of the liquid distributor 016 in the first direction), that is, at a position closer to the reaction zone 009 than to liquid distributor 016. Through the first mixing element 015, the liquid can be further mixed to improve the uniformity of mixing of the two groups of streams.

More specifically, the first mixing element 015 is provided with a main flow portion and a branch flow portion that are alternately arranged and in communication along the first direction. The main flow portion is provided with one main flow passage 0001, and the diverter flow portion is provided with a plurality of diverter flow passages 0002. As shown in FIG. 4, one or more main flow portions/diversion stream portions may accordingly be provided and arranged alternately, with only one main flow passage 0001 located in the main flow portion and a plurality of diversion flow passages 0002 located in the diversion stream portion. The liquid converges in the main flow passage 0001 and is distributed in the diverter flow passages 0002 of each part of the diverter flow. By such a convergence-distribution process, the degree of turbulence can be generally increased and the uniformity of liquid mixing can be improved.

In addition, in the first mixing element 015, a collection cavity 0003, which is in communication with a plurality of passages of the exhaust flow 0002, is located downstream of the portion of the exhaust flow 0002. As shown in FIG. 4, the volume (especially the cross-sectional area) of the collection cavity 0003 is larger than the volume (especially the cross-sectional area) of the main flow passage 0001, and the collection cavity 0003 can bring together a plurality of upstream diverter flow passages 0002, and this cavity is in communication with the next passing the main flow 0001 or with the next stage of the reaction zone 009 or transition zone 020.

In FIG. 4 shows a first mixing element 015 according to an embodiment of the present invention, which is formed by splicing a plurality of plate elements (the number may be 2-100, preferably 2-50, more preferably 10-30, and the thickness is approximately 0.2-10 mm) located along the first direction, and structures such as holes and cavities are formed on each plate member, which correspond to the main flow passage 0001, the exhaust flow passage 0002 and the collection cavity 0003, which is convenient for processing and production.

In addition, the mixing zone 008 includes a first heat exchange cavity located in the housing 003, a mixing channel 014 is located in the first heat exchange cavity 013, the housing 003 is provided with a first heat exchange medium inlet 004 and a first heat exchange medium outlet 005, which are in communication with the first heat exchange medium cavity 013. In the mixing zone 008, the mixing channel 014 and the first heat exchange cavity 013 are isolated from each other and are not in communication with each other, but heat transfer between them can be ensured, and pipe fittings with good thermal conductivity can be used in the mixing channel 014. By supplying the heat exchange medium to the first inlet of the heat exchange medium 004 and discharging the heat exchange medium through the first outlet of the heat exchange medium 005, a circulating flow of the heat exchange medium can be formed in the first heat exchange cavity 013 to realize heat exchange with the mixing channel 014 and the liquid therein, then is to realize the heat dissipation of the mixing channel 014 and the liquid therein, and to ensure that the heat generated by mixing and dissolving the liquid in the mixing channel 014 is dissipated over time, so that the liquid therein is in a suitable temperature range.

In addition, the volume ratio of the first heat exchange cavity 013 to the mixing channel 014 is 2-50; preferably, the volume ratio of the first heat exchange cavity 013 to the mixing channel 014 is 5-30. The volume of the first heat exchange cavity 013 is larger than the volume of the mixing channel 014, so that the heat generated due to the mixing and dissolution of the first reaction flow group and the second reaction flow group is removed in a timely manner.

In addition, a transition zone 020 is provided between the mixing zone 008 and the reaction zone 009, the transition zone 020 being provided with a stabilizing channel 021 with a constant cross-section and a diffusion channel 022 with a gradually increasing cross-section, which are located and in communication along the first direction; the stabilizing channel 021 is in communication with the mixing channel 014, and the diffusion channel 022 is in communication with the reaction zone 009. The transition zone 020 can bring together mixed liquids from a plurality of mixing channels 014 in the stabilizing channel 021 to achieve another uniform mixing, and then supply the mixed liquid into the reaction zone 009 through the diffusion channel 022. In addition, the transition zone 020 is equipped with a stabilizing channel 021 and a diffusion channel 022, the stabilizing channel 021 mainly realizes the convergence and mixing of liquids, and the diffusion channel 022 is shaped like a bell, which, for example, distributes the mixed liquid into a plurality of reaction channels 010, as described below. The two ends of the transition zone 020 are respectively provided with dividing walls with through holes so that they are isolated from the mixing zone 008 (mainly the first heat exchange cavity 013) and the reaction zone 009 (mainly the second heat exchange cavity 012) and are in communication with each mixing channel 014 and each parallel reaction channel 010 through each through hole on each partition wall, and the diffusion channel 022 and the stabilizing channel 021 may be pipe fittings provided between the two partition walls.

In addition, the stabilizing channel 021 can be connected to the outlet pipe 018 extending to the outside of the housing 003. As mentioned above, the stabilizing channel 021 has the function of convergence and mixing, and the outlet pipe 018 can release bubbles and flows accumulated in the stabilizing channel 021. to eliminate the influence of bubble accumulation on mixing uniformity and flow blocking. A valve can be installed on the outlet pipe 018, and the valve can be opened when bubbles or flows need to be released.

In addition, the diffusion channel 022 is provided with a diffusion plate with holes or slits. The diffusion plate may be substantially perpendicular to the first direction. The liquid in the diffusion channel 022 can flow through the cells or slits on the diffusion plate, so that the liquid is dispersed and the uniformity of the mixed liquid is improved.

More specifically, the reaction zone 009 is provided with a plurality of parallel reaction channels 010 extending along the first direction and in communication with the mixing channel 014 through the stabilizing channel 021 and the diffusion channel 022. The reaction channel 010 provides a reaction space for the mixed liquid and carries the mixed liquid so that it flowed to the next stage of the collection zone 024 along the first direction, so that the mixed liquid reacts while forming a stable piston flow 010 in the reaction channel to eliminate unwanted products due to the variability of the residence time distribution. As stated above, a transition zone 020 may be provided between the reaction zone 009 and the mixing zone 008, and a plurality of reaction channels 010 may be in communication with the diffusion channel 022, so that the mixed liquid in the diffusion channel 022 is uniformly distributed into the plurality of reaction channels 010. Amount reaction channels is, for example, 2-10000 channels, preferably 2-5000 channels and more preferably 2-500 channels. The reaction channel 010 may have a cross-section of at least one of circular, rectangular and triangular shapes.

In addition, the reaction channel 010 is provided with a second mixing element 011, and the second mixing element 011 includes a support bar 0004 extending along the first direction, and a toothed element 0005 connected to the support bar 0004 and extending transversely to the support bar 0004. In the second mixing element 011, the support bar 011 the bar 0004 provides support for a plurality of gear members 0005, so that the gear members 0005 can be stably held in the reaction channel 010, and the gear members 0005 extend approximately across the reaction channel 010, which can improve the degree of turbulence of the liquid in the reaction channel 010, thereby improving the uniformity of mixing between reaction streams.

In addition, the 0005 gear elements are in one of triangular, arcuate, wavy and spiral shapes. The toothed elements may have different shapes as they extend across the reaction channel 010 and may provide the effect of increasing the degree of turbulence of the liquid.

Preferably, the toothed element 0005 has a triangular shape, and on one side of the triangle adjacent to the support bar 0004, one corner is connected to the support bar 0004, and the other corner is spaced 0.01-20 mm from the support bar 0004. The toothed elements 0005 may be triangular plate elements and are connected to the support strip 0004 using only one corner.

Preferably, each reaction channel 010 is provided with a plurality of second mixing elements 011 (the number may be 2-100, preferably 2-50, more preferably 10-30), which are stacked on top of each other at intervals; and a plurality of second mixing elements 011 are stacked on each other at intervals, and accordingly the gear elements 0005 are also stacked on each other at intervals, and the gear elements 0005 of different second mixing elements 011 are arranged in a staggered manner, so that the different second mixing elements 011 are arranged more unevenly , and the degree of turbulence of the liquid in the reaction channel 010 can be improved to a greater extent.

Preferably, the cross-section of the reaction channel 010 is rectangular, and the toothed elements 0005 extend between a set of opposite sides of the rectangle. More specifically, the reaction channel 010 has four side walls, that is, two sets of opposite parallel side walls, a support bar 0004 is located on one side wall of the reaction channel 010, and toothed elements 0005 extend towards the other opposite side wall, and a plurality of second mixing elements 011 may better fit the structure of the inner cavity of the reaction channel 010, which has the shape of a square column.

More specifically, the reaction channel 010 has a cross-sectional area of 1-150 mm ² and a length of 50-5000 mm, the minimum distance between the reaction channels 010 is 1-50 mm, and the second mixing element 011 has a thickness of 0.1-3 mm, and the distance between adjacent toothed elements 0005 is 1-50 mm.

Preferably, the reaction channel 010 has a length of 100-3000 mm, the minimum gap between the reaction channels 010 is 3-30 mm, the second mixing element 011 has a thickness of 0.2-2 mm, the gap between adjacent toothed elements 0005 is 1.5-20 mm. The minimum spacing of the reaction channels 010 reflects the density of the reaction channels 010 in the reaction zone 009. Preferably, in the second mixing element 011, the gear element 0005 is a plate element, which may be coplanar with the support bar 0004, and the thickness of the second mixing element 011 is approximately equal to the thickness of the gear element 0005 .

In addition, the reaction zone 009 may be provided with a second heat exchange cavity 012 located in the housing 003; the reaction channel 010 is located in the second heat exchange cavity 012, the housing 003 is provided with a second heat-conducting medium inlet 006 and a second heat-conducting medium outlet 007, which are in communication with the second heat exchange cavity 012. The second heat exchange cavity 012 may be advantageously formed by the housing 003, and on At the two ends there are respectively a second dividing wall 025 between the reaction zone 009 and the collection zone 024 and a dividing wall between the reaction zone 009 and the transition zone 020. Through the second inlet opening of the heat-conducting medium 006 and the second outlet opening of the heat-conducting medium 007, the heat exchange medium can be introduced into the second heat exchange medium a cavity 012 for performing a heat exchange treatment on the reaction channel 010 to ensure that the liquid in the reaction channel 010 reacts within an appropriate temperature range and to prevent the production of undesirable products.

In addition, the first heat exchange cavity 013 and the second heat exchange cavity 012 may be connected to each other in series and located on the same heat exchange circulation flow path, or may also be located in parallel on the same heat exchange flow circulation path, or may be located on two different circulation paths heat transfer flow, respectively.

In addition, the volume ratio of the second heat exchange cavity 012 to the reaction channel 010 is 2-50; preferably, the volume ratio of the second heat exchange cavity 012 to the reaction channel 010 is 5-30. The volume of the second heat exchange cavity 012 is larger than the volume of the reaction channel 010, so that the heat in the reaction channel 010 can be removed in time to ensure a suitable temperature of the reaction channel 010.

The preferred microchannel reactor of the present invention can be used for the synthesis of polyalpha-olefin synthetic oil; supply pipe 002 can be used to introduce a liquid phase flow (continuous phase) (mixed flow from inlet unit 1), and liquid distribution pipe 017 can be used to introduce a gas phase flow (dispersive phase) (separately supplied BF ₃ catalyst from inlet unit 1 ). The liquid-phase flow is used as a continuous phase to be supplied to the feeding zone 023 of the microchannel reactor from the supply pipe 002, and the gas-phase flow is used as a dispersed phase to be supplied to the mixing channel 014 of the reactor from the liquid distribution pipe 017 and dissolved into the continuous phase by a distributor 016 liquids. The mixed liquid that has completely reacted in the reaction channel 010 enters the collection area 024 and is finally discharged from the outlet pipe 001.

In embodiments of the invention, preferred structural components or parameters are used without re-listing when the preferred microchannel reactor is used, unless otherwise noted.

In FIG. 7 is a schematic view of a comparative apparatus of the present invention, the apparatus including an inlet unit 1, a tubular reactor 2 and a post-treatment unit 3, which are connected in series; the inlet unit 1 includes a mixer 12 for auxiliary raw materials and olefin feedstock and a pipeline for separately supplying BF ₃ catalyst.

Example 1

In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; the stream obtained by mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the entire olefin feedstock is separately passed into the microchannel reactor (the setting mode 2 mentioned above and the feed mode 2 in accordance with this invention).

In installation, the mixer has the following structure and parameters: The mixer has a cylindrical structure with an outer diameter of 10 cm and an inner diameter of 6 cm. The mixer has two inlet holes for supply at the lower end and one outlet outlet for discharge at the very top end. The mixer is equipped with a layer of filler, and the filler is ceramic balls. The mixer contains a heat exchange layer having a temperature of 0-100°C.

In the installation, the microchannel reactor used is the preferred microchannel reactor of the present invention described above, containing 5 parallel reaction channels 010; each reaction channel 010 has a rectangular cross-section with a cross-sectional area of 20 mm ² , and the reaction channel 010 has a length of 2000 mm. The second mixing element 011 in the reaction channel 010 has triangular gear elements 0005, and the gap between adjacent tooth elements 0005 is 5 mm. A total of four layers of superimposed mixing elements 011 are arranged in the reaction channel 010, as shown in FIG. 5. The reactor contains two mixing channels 014, which have a cross-sectional area of 10 cm ² and a length of 800 mm. The liquid distributor 016 is a sintered metal powder body having an average pore size of 5 μm, a cross-sectional area of 8.5 cm ² and a length of 150 mm. Each mixing channel 014 is provided with three first mixing elements 015.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/h and n-butanol at 0.6 l/h are mixed in a mixer. Microchannel reactor 2 is supplied with each individual flow in a mixer at a flow rate of 1.2 l/hour, BF ₃ gas at a flow rate of 189 l/hour, which is additionally supplied separately, and decene at a flow rate of 60 l/hour. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 1.

Table 1

Olefin composition distribution Content Monomer, % 1.2 Dimer, % 3.1 Trimer, % 43.1 Tetramer, % 32.1 Pentamer, % 17.0 ≥Hexamer, % 3.5 Conversion, % 98.8

Example 2

In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; the stream obtained by mixing part of the BF ₃ catalyst and part of the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock and the entire olefin feedstock are separately passed into the microchannel reactor (the above-mentioned setting mode 3 and feed mode 3 in accordance with the present invention).

The mixer and microchannel reactor have the same structure as in example 1.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/h and n-butanol at 0.3 l/h are mixed in a mixer. Microchannel reactor 2 is supplied with each individual flow in a mixer at a flow rate of 1.2 l/hour, BF ₃ gas at a flow rate of 189 l/hour, which is additionally supplied separately, n-butanol at 0.3 l/hour and decene at a flow rate of 60 l/hour. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 2.

table 2

Olefin composition distribution Content Monomer, % 1.1 Dimer, % 3.5 Trimer, % 43.2 Tetramer, % 31.7 Pentamer, % 17.1 ≥Hexamer, % 3.4 Conversion, % 98.9

Example 3

In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; the stream obtained by mixing part of the BF ₃ catalyst, part of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock is separately passed into the microchannel reactor (the above-mentioned setting mode 4 and feed mode 4 in accordance with the present invention).

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 1.

In the installation, the mixer 11 has the following structure and parameters: the mixer has a cylindrical structure with an outer diameter of 10 cm and an inner diameter of 6 cm. The mixer has two supply inlets at the lower end and one outlet outlet at the uppermost end. The mixer is equipped with a layer of filler, and the filler is ceramic balls. The mixer contains a heat exchange layer having a temperature of 0-100°C.

In the installation, the mixer 12 has the following structure and parameters: the mixer has a cylindrical structure with an outer diameter of 10 cm and an inner diameter of 6 cm. The mixer has two supply inlets at the lower end and one outlet outlet at the uppermost end. The mixer is provided with a layer of filler, and the filler is ordinary filler. The mixer contains a heat exchange layer having a temperature of 0-50°C.

The microchannel reactor has the same structure as in example 1.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.3 l/hour are mixed in mixer 11, and then the mixture and decene at a flow rate of 60 l/hour are mixed in mixer 12. Each is supplied to microchannel reactor 2 separately, the flow in mixer 12 at a flow rate of 60.6 l/hour, BF ₃ gas at a flow rate of 189 l/hour, which is additionally supplied separately, and n-butanol at 0.3 l/hour. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 3.

Table 3

Olefin composition distribution Content Monomer, % 0.9 Dimer, % 2.9 Trimer, % 43.2 Tetramer, % 32.3 Pentamer, % 17.0 ≥Hexamer, % 3.7 Conversion, % 99.1

Example 4

In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; the stream obtained by mixing part of the BF ₃ catalyst, all of the auxiliary feedstock and part of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the olefin feedstock is separately passed into the microchannel reactor (the above-mentioned setting mode 5 and feed mode 5 in accordance with the present invention).

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 1.

The mixer and microchannel reactor have the same structure as in example 3.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and then the mixture and decene at a flow rate of 30 l/hour are mixed in mixer 12. Each is supplied to microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 30.6 l/hour, BF ₃ -gas at a flow rate of 189 l/hour, which is additionally supplied separately, and decene at 0.3 l/hour. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 4.

Table 4

Olefin composition distribution Content Monomer, % 1.7 Dimer, % 3.7 Trimer, % 42.6 Tetramer, % 32.1 Pentamer, % 16.6 ≥Hexamer, % 3.3 Conversion, % 98.3

Example 5

In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; the stream obtained by mixing part of the BF ₃ catalyst, all of the auxiliary raw material and all of the olefin feedstock is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor (the above-mentioned setting mode 6 and feed mode 6 in accordance with the present invention).

The mixer and microchannel reactor have the same structure as in Example 1, except that the mixer used has three feed inlets.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/h, n-butanol at 0.6 l/h and decene at a flow rate of 60 l/h are passed into the mixer for mixing. Microchannel reactor 2 is supplied with each individual flow in the mixer at a flow rate of 61.2 l/hour and BF ₃ gas at a flow rate of 189 l/hour, which is additionally supplied separately. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 5.

Table 5

Olefin composition distribution Content Monomer, % 0.7 Dimer, % 2.5 Trimer, % 43.3 Tetramer, % 32.4 Pentamer, % 17.2 ≥Hexamer, % 3.9 Conversion, % 99.3

Example 6

In this example, the weight ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer for mixing is 60:40. At the inlet section, a portion of the BF ₃ catalyst and all auxiliary feedstocks are first mixed, then subjected to a second mixing with all of the olefin feedstock, then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor (the above setting mode 6 and feed mode 6 in accordance with the present invention).

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 2.

The mixer and microchannel reactor have the same structure as in example 3.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and the mixed stream and decene at a flow rate of 60 l/hour are passed into mixer 12. Each is fed into microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 189 l/hour, which is additionally supplied separately. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 6.

Table 6

Olefin composition distribution Content Monomer, % 0.2 Dimer, % 1.9 Trimer, % 43.9 Tetramer, % 32.2 Pentamer, % 18.0 ≥Hexamer, % 3.8 Conversion, % 99.8

Example 7

In this example, the weight ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 50:50. At the inlet, a portion of the BF ₃ catalyst and all of the auxiliary feedstocks are first mixed, then second mixed with all of the olefin feedstock, then the mixed stream is passed into the microchannel reactor, and the remainder of the BF3 catalyst is separately passed into the microchannel reactor.

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 2.

The mixer and microchannel reactor have the same structure as in example 3.

In the installation, the post-processing unit 3 is a solid adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the tank with potassium oxide.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and the mixed stream and decene at a flow rate of 60 l/hour are passed into mixer 12. Each is fed into microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 126 l/hour, which is additionally supplied separately. The polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the alkaline washing and aqueous washing devices for subsequent processing. The polyolefin product is obtained after removal of the catalyst. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 7.

Table 7

Olefin composition distribution Content Monomer, % 0.9 Dimer, % 2.2 Trimer, % 43.3 Tetramer, % 32.5 Pentamer, % 17.3 ≥Hexamer, % 3.8 Conversion, % 99.1

Comparative example 1

Olefin polymerization is carried out using the polyalphaolefin production plant shown in FIG. 2. In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; a portion of the BF ₃ catalyst and all auxiliary feedstocks are first mixed, then subjected to a second mixing with all of the olefin feedstock, then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor.

The mixer has the same structure as the mixer of example 3.

In the setup, the microchannel reactor 2 has 5 parallel reaction channels 010, each reaction channel 010 has a rectangular cross-section with a cross-sectional area of 20 mm ² , and the reaction channel 010 has a length of 2000 mm. The second mixing element 011 in the reaction channel 010 has triangular gear elements 0005, and the gap between adjacent tooth elements 0005 is 5 mm. In the reaction channel 010, a total of four layers of superimposed mixing elements 011 are arranged, as shown in FIG. 5. The reactor has neither a mixing channel 014 nor a liquid distributor 016.

In the installation, the post-processing unit 3 is an adsorption device and has the following structure and parameters: open type device, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the adsorption device with calcium oxide.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and the mixed stream and decene at a flow rate of 60 l/hour are passed into mixer 12. Each is fed into microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 189 l/hour, which is additionally supplied separately. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained after the polymerization reaction enters the adsorption device, and the catalyst is removed by absorption to obtain a polyolefin product. A small amount of sample is taken and measurements are carried out using gas chromatography to determine the content of each component in the product. The test results are shown in Table 8.

Table 8

Olefin composition distribution Content Monomer, % 19.4 Dimer, % 13.2 Trimer, % 23.9 Tetramer, % 23.4 Pentamer, % 14.5 ≥Hexamer, % 5.6 Conversion, % 80.6

Comparative example 2

The polymerization reaction is carried out using the polyalphaolefin production plant shown in FIG. 2. In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40; a portion of the BF ₃ catalyst and all auxiliary feedstocks are first mixed, then subjected to a second mixing with all of the olefin feedstock, then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor.

The microchannel reactor has the same structure as in example 3.

In the setup, the microchannel reactor 2 has 5 parallel reaction channels 010, each reaction channel 010 has a rectangular cross-section with a cross-sectional area of 20 mm ² , and the reaction channel 010 has a length of 2000 mm. The second mixing element 011 in the reaction channel 010 has triangular gear elements 0005, and the gap between adjacent tooth elements 0005 is 5 mm. In the reaction channel 010, a total of four layers of superimposed mixing elements 011 are arranged, as shown in FIG. 5. The reactor has one mixing channel 014, which has a cross-sectional area of 10 cm ² and a length of 800 mm. The liquid distributor 016 is a sintered metal powder body having an average pore size of 5 μm, a cross-sectional area of 8.5 cm ² and a length of 150 mm. Three first mixing elements 015 are provided in the mixing channel 014.

In the installation, the post-processing unit 3 is a centrifugation device and has the following structure and parameters: tubular centrifuge, operates at normal temperature and the separation coefficient is 8000G.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and the mixed stream and decene at a flow rate of 60 l/hour are passed into mixer 12. Each is fed into microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 189 l/hour, which is additionally supplied separately. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained from the polymerization reaction is sent to a centrifugation device, separated by centrifugation to remove the catalyst, washed three times with water, and a polyolefin product is obtained. Once the system is running stable, a small amount of sample is taken and measurements are carried out using gas chromatography to determine the content of each component in the product. The test results are shown in Table 9.

Table 9

Olefin composition distribution Content Monomer, % 15.5 Dimer, % 7.8 Trimer, % 32.5 Tetramer, % 26.8 Pentamer, % 13.2 ≥Hexamer, % 4.2 Conversion, % 84.5

Example 8

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 2. In this example, the mass ratio of BF ₃ directly fed into the microchannel reactor to BF ₃ fed into the mixer to participate in mixing is 60:40. At the inlet, a portion of the BF ₃ catalyst and all of the auxiliary feedstocks are first mixed, then subjected to a second mixing with all of the olefin feedstock, then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor.

The mixer and microchannel reactor have the same structure as in example 3.

In the setup, the microchannel reactor 2 has 5 parallel reaction channels 010, each reaction channel 010 has a rectangular cross-section with a cross-sectional area of 20 mm ² , and the reaction channel 010 has a length of 2000 mm. The second mixing element 011 in the reaction channel 010 has triangular gear elements 0005, and the gap between adjacent tooth elements 0005 is 5 mm. In the reaction channel 010, a total of four layers of superimposed mixing elements 011 are arranged, as shown in FIG. 5. The reactor contains two mixing channels 014, which have a cross-sectional area of 10 cm ² and a length of 800 mm. Each mixing channel 014 is provided with three first mixing elements 015. The liquid distributor 016 is made of micro/mesoporous tubular material, and the hollow microchannels constituting the mesh frame of the micro/mesoporous tubular material have a cross-sectional area of 8.5 cm ² and an average pore diameter of 2 µm and length 150 mm.

In the installation, the post-processing unit 3 is a centrifugation device and has the following structure and parameters: tubular centrifuge, operates at normal temperature and the separation coefficient is 8000G.

BF ₃ -Gas at a flow rate of 126 l/hour and n-butanol at 0.6 l/hour are mixed in mixer 11, and the mixed stream and decene at a flow rate of 60 l/hour are passed into mixer 12. Each is fed into microchannel reactor 2 separately the flow in mixer 12 at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 189 l/hour, which is additionally supplied separately. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained from the polymerization reaction is sent to a centrifugation device, separated by centrifugation to remove the catalyst, washed three times with water, and a polyolefin product is obtained. Once the system is running stable, a small amount of sample is taken and measurements are carried out using gas chromatography to determine the content of each component in the product. The test results are shown in Table 10.

Table 10

Olefin composition distribution Content Monomer, % 0.6 Dimer, % 2.7 Trimer, % 42.6 Tetramer, % 31.7 Pentamer, % 18.3 ≥Hexamer, % 4.1 Conversion, % 99.4

Comparative example 3

In this example, the structure and parameters of microchannel reactor 2 are identical to the structure and parameters of example 1.

In the installation, the post-processing unit 3 is an adsorption device and has the following structure and process parameters: open type, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the adsorption device with calcium oxide.

Microchannel reactor 2 is supplied individually with BF ₃ gas at a flow rate of 315 l/hour, n-butanol at 0.6 l/hour and decene at a flow rate of 60 l/hour. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The resulting reaction stream enters an adsorption device, the catalyst is removed by absorption, and a polyolefin product is obtained. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 11.

Table 11

Olefin composition distribution Content Monomer, % 7.4 Dimer, % 6.9 Trimer, % 38.1 Tetramer, % 29.5 Pentamer, % 15.9 ≥Hexamer, % 2.2 Conversion, % 92.6

Comparative example 4

In this example, the structure and parameters of the mixer and microchannel reactor 2 are identical to the structure and parameters in example 1.

In the installation, the post-processing unit 3 is an adsorption device and has the following structure and process parameters: open type, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the adsorption device with calcium oxide.

BF ₃ -Gas at a flow rate of 315 l/h and n-butanol at 0.6 l/h are mixed in a mixer. The mixed stream and decene at a flow rate of 60 l/h are each separately supplied to the microchannel reactor 2. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The resulting reaction stream enters an adsorption device, the catalyst is removed by absorption, and a polyolefin product is obtained. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 12.

Table 12

Olefin composition distribution Content Monomer, % 5.5 Dimer, % 2.8 Trimer, % 40.5 Tetramer, % 28.8 Pentamer, % 18.2 ≥Hexamer, % 4.2 Conversion, % 94.5

Comparative Example 5

In this example, the structure and parameters of the mixer and microchannel reactor 2 are identical to the structure and parameters in example 1.

In the installation, the post-processing unit 3 is an adsorption device and has the following structure and process parameters: open type, effective volume 10 L, operating at normal temperature, feeding at the lower end, discharging at the upper end, and filling the adsorption device with calcium oxide.

n-Butanol at 0.6 l/h and decene at a flow rate of 60 l/h are mixed in a mixer. The mixed stream at a flow rate of 61.2 l/h and BF ₃ gas at a flow rate of 315 l/h are each separately supplied to the microchannel reactor 2. In the microchannel reactor 2, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The stream obtained from the polymerization reaction enters the adsorption device, the catalyst is removed by absorption, and a polyolefin product is obtained. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 13.

Table 13

Olefin composition distribution Content Monomer, % 1.9 Dimer, % 2.7 Trimer, % 43.2 Tetramer, % 32.1 Pentamer, % 15.6 ≥Hexamer, % 4.5 Conversion, % 98.1

Comparative Example 6

Polymerization of the olefin feedstock is carried out using the polyalphaolefin production plant shown in FIG. 7.

In the installation, the mixer has the same structure and parameters as in example 1.

In the apparatus, the tubular reactor includes a reaction tube and a hollow cylindrical body for housing a heat exchange medium, and the reaction tube is located in the hollow cylindrical body in the shape of a spiral coil. The baffles are arranged in the hollow cylindrical body at intervals along the circumferential direction, the baffles extending along the cross-sectional direction of the reaction tubes and are provided with through holes capable of receiving the reaction tubes, so that the reaction tubes extend through the baffles. The cylindrical body is provided with a heat exchange medium inlet and a heat exchange medium outlet, respectively.

In the installation, the post-processing unit is an adsorption device that has the same structure and technological parameters as in example 3.

n-Butanol at 0.6 l/hour and decene at a flow rate of 60 l/hour are mixed in mixer 12. Mixed flow at a flow rate of 61.2 l/hour and BF ₃ -gas at a flow rate of 315 l/hour each separately supplied to the microchannel reactor 2. In the tubular reactor, a polymerization reaction occurs, the reaction temperature is 20°C, and the pressure is 5 MPa. The resulting reaction stream enters an adsorption device, the catalyst is removed by absorption, and a polyolefin product is obtained. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 14.

Table 14

Olefin composition distribution Content Monomer, % 22.7 Dimer, % 6.3 Trimer, % 25.1 Tetramer, % 22.2 Pentamer, % 14.6 ≥Hexamer, % 9.1 Conversion, % 77.3

Comparative example 7

In this example, the structure and parameters of the mixer and microchannel reactor 2 are identical to the structure and parameters in example 1.

BF ₃ -Gas at a flow rate of 5 l/hour and n-butanol at 0.6 l/hour are mixed in a mixer, the mixed stream is passed into microchannel reactor 2, and 1-decene at a flow rate of 30 l/hour is passed into microchannel reactor 2 The polymerization reaction occurs in the microchannel reactor, the reaction temperature is 20ºC, and the pressure is 5 MPa. The stream obtained from the polymerization reaction enters the adsorption device, the catalyst is removed by absorption, and a polyolefin product is obtained. Once the system is running stable, a sample is taken and measurements are taken using gas chromatography to determine the content of each component in the product. The test results are shown in Table 15.

Table 15

Olefin composition distribution Content Monomer, % 33.5 Dimer, % 12.9 Trimer, % 25.6 Tetramer, % 14.7 Pentamer, % 9.2 ≥Hexamer, % 4.1 Conversion, % 66.5

The polyolefin products of Examples 1-8 and Comparative Examples 1-7 are distilled and fractionated to produce polyalpha-olefin synthetic oils above 280°C and determine the kinematic viscosity at 100°C and the viscosity index. The results are presented in table Table 16.

Table 16

Efficiency mark Kinematic viscosity at 100°C, mm ² /sec Viscosity index Example 1 5,154 141 Example 2 5.201 143 Example 3 5.223 144 Example 4 5,163 143 Example 5 5,364 144 Example 6 5.728 148 Example 7 5,248 146 Example 8 5.295 149 Comparative example 1 4,167 134 Comparative example 2 4.124 135 Comparative example 3 4,277 134 Comparative example 4 4,251 136 Comparative Example 5 4,769 139 Comparative Example 6 4.617 135 Comparative example 7 4,316 129

From the above examples and comparative examples, it can be seen that by using the specific process of the present invention for producing polyalphaolefin synthetic oil, the conversion to the target product can be improved. In addition, when using the preferred microchannel reactor, the method for synthesizing polyalphaolefin synthetic oil has a high conversion. This is because the reaction channel 010 and the mixing channel 014 are both tubular structures arranged in the same direction, so that the mixed liquid can form a stable piston flow along the first direction, improving the consistency of the residence time of the mixed liquid and eliminating or reducing the formation of undesirable products . In addition, the reaction channel 10 is provided with a second mixing element 011, and the mixing channel 014 is provided with a liquid distributor 016 and a first mixing element 015, which can further improve the degree of turbulence of the mixed liquid, improve mixing uniformity, and eliminate or reduce the production of undesirable products and improve conversion into the target product.

Moreover, from the above examples and comparative examples, it can be seen that by using the method of the present invention for producing polyalphaolefin synthetic oil, a polyalphaolefin synthetic oil with excellent characteristics in both kinematic viscosity and viscosity index can be obtained.

Preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the invention, various simple modifications can be made to the technical solutions of the invention in any suitable manner, including combinations of various specific technical characteristics. To avoid unnecessary repetition, the different possible combinations are not described in detail here. However, these simple modifications and combinations should also be considered as the disclosed content of the invention, and all of them fall within the scope of protection of the present invention.

Claims (73)

1. An installation for producing polyalphaolefins, including an inlet unit (1), a microchannel reactor (2) and a post-processing unit (3), which are connected in series, the inlet unit including a mixer and/or pipeline(s) for supplying olefin feedstock, auxiliary raw materials and BF ₃ catalyst into the microchannel reactor (2), the inlet unit (1) contains at least a mixer for mixing at least part of the auxiliary raw material and at least part of the BF ₃ catalyst and a pipeline for separately supplying at least part of the BF ₃ catalyst into the microchannel reactor ( 2). 2. Installation according to claim 1, which differs in that the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and a portion of the olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the remainder of the olefin feedstock, based on the type of feedstock, into microchannel reactor (2); or the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock, a conduit for separately passing the remainder of the BF ₃ catalyst into the microchannel reactor (2), and a conduit for separately passing all of the olefin feedstock into the microchannel reactor (2); or the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst and a portion of the auxiliary feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the entire olefin feedstock into the microchannel reactor (2); or the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and all of the olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock into the microchannel reactor (2); or the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and a portion of the olefin feedstock, and conduits for separately passing each of the remainder of the BF ₃ catalyst and the remainder of the olefin feedstock into the microchannel reactor (2); or the inlet assembly (1) includes a mixer for mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock and all of the olefin feedstock, and a conduit for separately passing the remainder of the BF ₃ catalyst into the microchannel reactor (2); in the case where the BF ₃ catalyst, the auxiliary feedstock and the olefin feedstock are mixed in the inlet unit, the inlet unit includes a first mixer for mixing any two of the above three feedstocks, and a second mixer for mixing a mixture of the first mixer and the remaining one feedstock, at in this case, the first mixer is in communication with the second mixer, and the second mixer is in communication with the microchannel reactor (2). 3. Installation according to any one of paragraphs. 1 and 2, which differs in that the microchannel reactor (2) includes: body (003); the supply zone (023), the mixing zone (008), the reaction zone (009) and the collection zone (024) are located in series and are in communication along the first direction in the housing (003), and the housing (003) is provided with a supply pipe (002), in communication with the supply zone (023), and an outlet pipe (001) in communication with the collection zone (024), and the mixing zone (008) is equipped with a mixing channel (014) running along the first direction; pipe (017) for liquid distribution; wherein a liquid distribution pipe (017) extends from the outside of the housing (003) into the mixing channel (014), the liquid distribution pipe (017) is connected to a liquid distributor (016) at the end of the mixing channel (014); a supply pipe (002) is configured to be used for introducing feedstock from the inlet unit, and a liquid distribution pipe (017) is connected to a pipeline for separately supplied BF ₃ catalyst of the inlet unit (1) and can be used to introduce BF ₃ catalyst, the outlet pipe (001) is connected to the post-processing unit (3). 4. Installation according to claim 3, which differs in that the liquid distributor is at least one selected from a micropore powder sintered body, a mesoporous foam, a wire mesh, and a microslit or micropore tube; and/or the mixing zone is provided with 2-100 mixing channels, the liquid distribution pipe includes a main pipe extending from the outside of the housing into the supply zone, and branch pipes extending from the supply zone into each mixing channel with liquid distributors connected to the ends of the branch pipes, preferably a mixing channel the channel has a circular cross-section; and/or in the mixing channel, the first mixing element is located downstream of the liquid distributor; and/or the first mixing element is provided with a main flow portion and a waste flow portion that are alternately arranged and in communication along the first direction, the main flow portion being provided with a single main flow passage, and the waste flow portion being provided with a plurality of exhaust flow passages; and/or a collection cavity in communication with a plurality of diversion flow passages is located downstream of the diversion flow portion; and/or the mixing zone contains a first heat exchange cavity located in the housing, a mixing channel is located in the first heat exchange cavity, the housing is equipped with a first heat exchange medium inlet and a first heat exchange medium outlet, which are in communication with the first heat exchange cavity; and/or the volumetric ratio of the first heat exchange cavity to the mixing channel is 2-50; and/or a transition zone is provided between the mixing zone and the reaction zone, wherein the transition zone is provided with a stabilizing channel with a constant cross-section and a diffusion channel with a gradually increasing cross-section, which are located and in communication along the first direction, the stabilizing channel is in communication with the mixing channel, diffusion the channel is in communication with the reaction zone; and/or an exhaust pipe extending to the outside of the housing is connected to a stabilizing channel; and/or the diffusion channel is equipped with a diffusion plate with holes or slits; and/or the reaction zone is equipped with a plurality of parallel reaction channels; and/or the reaction channel is provided with a second mixing element, and the second mixing element includes a support bar extending along the first direction, and a toothed element connected to the support bar and extending across the support bar; and/or the toothed element has at least one of triangular, arcuate, wavy and spiral shapes; and/or each of the reaction channels is independently provided with a plurality of second mixing elements that are stacked on top of each other at intervals, and the gear elements of the second mixing element are staggered with respect to each other; and/or the reaction channel has a cross-section of at least one of circular, rectangular and triangular shapes; and/or the reaction channel has a cross-sectional area of 1-150 mm ² and a length of 50-5000 mm, the minimum distance between the reaction channels is 1-50 mm, and the second mixing element has a thickness of 0.1-3 mm, and the gap between adjacent gear elements is 1 -50 mm; and/or the reaction zone is provided with a second heat exchange cavity located in the housing, the reaction channel is located in the second heat exchange cavity, the housing is equipped with a second heat exchange medium inlet and a second heat exchange medium outlet, which are in communication with the second heat exchange cavity; and/or the volumetric ratio of the second heat exchange cavity to the reaction channel is 2-50. 5. Installation according to any one of paragraphs. 1-4, which differs in that the post-processing unit (3) makes it possible to subject the incoming stream to subsequent processing to obtain a polyolefin product and the post-processing unit (3) represents one or more devices from an adsorption device, an extraction device, a distillation device, a centrifugation device, a sedimentation device, an alkaline device washing and water washing devices. 6. Installation according to any one of paragraphs. 1-5, which differs in that, based on the total mass of BF ₃ in the microchannel reactor (2), the mass ratio of the BF ₃ catalyst, which is directly fed into the microchannel reactor (2), to the BF ₃ catalyst, which is mixed in the inlet unit, is 90-10:10-90. 7. Installation according to any one of paragraphs. 3-4, which differs in that the liquid distributor is a cylindrical powder sintered body with micropores and the liquid distributor has a cross-sectional area of 0.01-200 cm ² and a length of 1-2000 mm, the mixing zone is provided with 2-50 mixing channels, the liquid distribution pipe includes a main pipe extending from the outside of the housing to the supply zone, and branch pipes extending from the supply zone to each mixing channel with liquid distributors connected to the ends of the branch pipes, the mixing channel has a circular cross-section and the mixing channel has a cross-sectional area of 0.05-400 cm ² and a length of 50-5000 mm, the volume ratio of the first heat exchange cavity to the mixing channel is 5-30, and/or the reaction zone is equipped with a plurality of parallel reaction channels 2-5000 channels running along the first direction and in communication with the mixing channel through the transition zone; and/or the gear element has a triangular shape, and on one side of the triangle adjacent to the support bar, one corner is connected to the support bar and the other corner is spaced 0.01-20 mm from the support bar, and/or the reaction channel has a cross-section of at least one of circular, rectangular and triangular shapes and the cross-section of the reaction channel is rectangular and the toothed elements extend between a set of opposite sides of the rectangle, the reaction channel has a cross-sectional area of 1-150 mm ² and a length of 100-3000 mm, the minimum distance between the reaction channels is 3-30 mm, and the second mixing element has a thickness of 0.2-2 mm, and the gap between adjacent gear elements is 1 .5-20 mm, and/or the volumetric ratio of the second heat exchange cavity to the reaction channel is 5-30. (preferred features of clause 4) 8. Installation according to any one of paragraphs. 1-5, which differs in that, based on the total mass of BF ₃ in the microchannel reactor (2), the mass ratio of the BF ₃ catalyst, which is directly fed into the microchannel reactor (2), to the BF ₃ catalyst, which is mixed in the inlet unit, is 70-50:30-50. (preferred feature item 5) 9. A method for producing polyalphaolefins, including: passing BF ₃ catalyst, auxiliary raw materials and olefin feedstock into a microchannel reactor through an inlet unit and conducting a polymerization reaction in the microchannel reactor, followed by further post-processing to obtain a polyolefin product, while in the inlet unit, in the microchannel reactor the weight ratio of auxiliary feedstock, olefin feedstock and BF ₃ catalyst is ultimately 1:1-1000:1-500. 10. The method according to claim 9, which differs in that at the inlet assembly, a portion of the BF ₃ catalyst, a portion of the auxiliary feedstock, and a portion of the olefin feedstock are mixed and then passed into the microchannel reactor, and the remaining BF ₃ catalyst, the remaining auxiliary feedstock, and the remaining olefin feedstock, based on the type of feedstock, are passed separately into the microchannel reactor reactor; or at the inlet portion, the stream obtained by mixing a portion of the BF ₃ catalyst and all of the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the entire olefin feedstock is separately passed into the microchannel reactor; or at the inlet portion, the stream obtained by mixing a portion of the BF ₃ catalyst and a portion of the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the entire olefin feedstock are passed separately into the microchannel reactor; or at the inlet portion, the stream obtained by mixing part of the BF ₃ catalyst, part of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock is passed separately into the microchannel reactor; or at the inlet portion, the stream obtained by mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and a portion of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the olefin feedstock is passed separately into the microchannel reactor; or at the inlet section, the stream obtained by mixing part of the BF ₃ catalyst, all of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor, at the inlet section, a portion of the BF ₃ catalyst and all the auxiliary feedstocks are first mixed in the first mixer, then subjected to a second mixing in the second mixer, and then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor. 11. The method of claim 9, wherein the olefin in the olefin feedstock is one or more C ₃ -C ₂₀ alpha olefins; optionally, the olefin feedstock further contains a mixture of C ₅ -C ₂₀ alkanes and/or a C ₁ -C ₂₀ oxygen-containing compound; and/or the auxiliary raw material is one or more of an alcohol having a carbon number of 1-20, an ether having a carbon number of 1-20, an aldehyde having a carbon number of 1-20, a ketone having a carbon number of 1-20 , an ester having a carbon number of 1-30, a carboxylic acid having a carbon number of 1-20, and a phenol having a carbon number of 1-20. 12. Method according to any one of paragraphs. 9-11, which is characterized in that the reaction temperature in the microchannel reactor is 0-120°C; the reaction pressure in the microchannel reactor is 0.01-10 MPa; The residence time of the olefin feedstock in the microchannel reactor is 1-3600 sec. 13. Method according to any one of paragraphs. 9-12, which differs in that, based on the total mass of BF ₃ in the microchannel reactor, the mass ratio of the BF ₃ catalyst separately supplied to the microchannel reactor to the BF ₃ catalyst, which is mixed in the inlet unit, is 90-10:10-90 . 14. Method according to any one of paragraphs. 9-13, which is characterized in that the post-processing method is one or more of adsorption, centrifugation, sedimentation, alkaline washing, water washing and gas-liquid separation methods; in the case where the post-processing method is sedimentation or centrifugation, optionally the resulting heavy liquid phase is returned to the inlet unit or microchannel reactor to continue to participate in the continuous reaction. 15. Method according to any one of paragraphs. 9-14, which is characterized in that the polyalphaolefin is produced by using a plant for producing polyalphaolefins according to any one of claims. 1-6. 16. The method according to claim 7, which differs in that at the inlet section, the stream obtained by mixing part of the BF ₃ catalyst and all the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the entire olefin feed material is separately passed into the microchannel reactor, and in the case of mixing part of the BF ₃ catalyst and of all auxiliary raw materials in the mixer, the flow rate of part of the BF ₃ catalyst into the mixer is 1-100,000 l/h, the flow rate of all auxiliary raw materials into the mixer is 0.01-1000 l/h, the flow rate of the mixture obtained after mixing part of the BF ₃ catalyst and of all auxiliary raw materials in the mixer, into the microchannel reactor is 0.01-2000 l/hour, the rate of passage of the BF ₃ catalyst residue separately into the microchannel reactor is 1-150000 l/hour, the rate of passage of the entire olefin feed material separately into the microchannel reactor is 10- 5000 l/hour; or at the inlet portion, the stream obtained by mixing part of the BF ₃ catalyst and part of the auxiliary feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst, the remainder of the auxiliary feedstock, and the entire olefin feedstock is passed separately into the microchannel reactor and, in the case of mixing, BF ₃ catalyst and part of the auxiliary raw material in the mixer, the flow rate of part of the BF ₃ catalyst into the mixer is 1-100000 l/h, the flow rate of part of the auxiliary raw material into the mixer is 0.01-800 l/h, the flow rate of the mixture obtained by mixing part BF ₃ catalyst and part of the auxiliary raw material in the mixer into the microchannel reactor is 0.01-1600 l/hour, the rate of passage of the remainder of the BF ₃ catalyst separately into the microchannel reactor is 1-120000 l/hour, the rate of passage of the remainder of the auxiliary raw material into the mixer is 0 .01-200 l/h, the flow rate of the entire olefin feed material separately into the microchannel reactor is 10-5000 l/h; or at the inlet section, the stream obtained by mixing part of the BF ₃ catalyst, part of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock is passed separately into the microchannel reactor and, in the case of mixing, part of the BF ₃ catalyst, part of the auxiliary raw material and all of the olefin feedstock in the mixer, the flow rate of the BF ₃ catalyst part into the mixer is 1-100,000 l/hour; the flow rate of part of the auxiliary raw material into the mixer is 0.01-800 l/hour; the flow rate of the total olefin feed material into the mixer is 10-5000 l/h; the flow rate of the mixture obtained by mixing, part of the BF ₃ catalyst, part of the auxiliary raw material and the entire olefin feedstock in the mixer into the microchannel reactor is 0.01-6000 l/h; the rate of separate passage of the remainder of the BF3 catalyst into the microchannel reactor is 1-150000 l/hour, the rate of passage of the remainder of the auxiliary raw material separately into the microchannel reactor is 0.01-200 l/hour; or at the inlet section, the stream obtained by mixing part of the BF ₃ catalyst, part of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the auxiliary feedstock is passed separately into the microchannel reactor and, in the case of mixing, part of the BF ₃ catalyst, part of the auxiliary raw material and all of the olefin feedstock in the mixer, the flow rate of the BF ₃ catalyst part into the mixer is 1-100,000 l/hour; the flow rate of part of the auxiliary raw material into the mixer is 0.01-800 l/hour; the flow rate of the total olefin feed material into the mixer is 10-5000 l/h; the flow rate of the mixture obtained by mixing, part of the BF ₃ catalyst, part of the auxiliary raw material and the entire olefin feedstock in the mixer into the microchannel reactor is 0.01-6000 l/h; the rate of separate passage of the remainder of the BF3 catalyst into the microchannel reactor is 1-150000 l/hour, the rate of passage of the remainder of the auxiliary raw material separately into the microchannel reactor is 0.01-200 l/hour; or at the inlet portion, the stream obtained by mixing a portion of the BF ₃ catalyst, all of the auxiliary feedstock, and a portion of the olefin feedstock is passed into a microchannel reactor, and each of the remainder of the BF ₃ catalyst and the remainder of the olefin feedstock is passed separately into the microchannel reactor and, in the case of mixing a portion BF ₃ catalyst, all the auxiliary raw materials and part of the olefin feedstock in the mixer, the flow rate of the BF ₃ catalyst part into the mixer is 1-100000 l/h, the flow rate of all the auxiliary raw materials into the mixer is 0.01-1000 l/h, the flow rate part of the olefin feedstock into the mixer is 1-2000 l/h, the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst, all the auxiliary raw materials and part of the olefin feedstock in the mixer into the microchannel reactor is 0.01-3000 l/h, the rate of individual passage of the remainder of the BF ₃ catalyst into the microchannel reactor is 1-150,000 L/hour, the rate of passage of the remainder of the olefin starting material separately into the microchannel reactor is 9-3,000 L/hour; or at the inlet section, the stream obtained by mixing part of the BF ₃ catalyst, all of the auxiliary feedstock and all of the olefin feedstock is passed into the microchannel reactor and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor and in the case of mixing part of the BF ₃ catalyst, all of the auxiliary feedstock and all olefin feedstock in the mixer, the flow rate of part of the BF ₃ catalyst into the mixer is 1-100000 l/h, the flow rate of the entire auxiliary raw material into the mixer is 0.01-1000 l/h, the flow rate of the entire olefin feedstock into the mixer is 10-5000 l/hour, the flow rate of the mixture obtained by mixing part of the BF ₃ catalyst, all the auxiliary raw materials and all the olefin starting material in the mixer into the microchannel reactor is 10-6000 l/hour, the flow rate of the remainder of the BF3 catalyst separately into the microchannel reactor is 1- 150000 l/hour; or at the inlet section, a portion of the BF ₃ catalyst and all auxiliary feedstocks are first mixed in a first mixer, then subjected to a second mixing in a second mixer with all of the olefin feed, and then the mixed stream is passed into the microchannel reactor, and the remainder of the BF ₃ catalyst is separately passed into the microchannel reactor ; Preferably, when the catalyst portion BF ₃ and all the auxiliary raw materials are first mixed in the first mixer, the flow rate of the catalyst portion BF ₃ into the first mixer is 1-100,000 l/h, the flow rate of the entire auxiliary raw material into the first mixer is 0.01-1000 l/h hour, wherein the stream obtained after the first mixing is then subjected to a second mixing with all of the olefin feed material in a second mixer, and the flow rate of the stream obtained after the first mixing into the second mixer is 0.01-2000 l/hour, the flow rate of the total olefin feedstock into the second mixer is 10-5000 l/h, the flow rate obtained after the second mixing into the microchannel reactor is 10-7000 l/h, the flow rate of the BF ₃ catalyst residue separately into the microchannel reactor is 1-150000 l/h hour. 17. Method according to any one of paragraphs. 9-12, which differs in that, based on the total mass of BF ₃ in the microchannel reactor, the mass ratio of the BF ₃ catalyst, separately supplied to the microchannel reactor, to the BF ₃ catalyst, which is mixed in the inlet unit, is 70-50:30-50 .

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