Production system of alpha-olefin

Abstract

The utility model relates to the technical field of alpha-olefin synthesis, and particularly provides a production system of alpha-olefin. The problem that in the prior art, when alpha-olefin is produced through oligomerization, generated polyethylene oligomer is prone to being accumulated on the surface of the pipe wall of a reaction system is solved. The alpha-olefin production system comprises a reaction unit, a sleeve heat exchange unit, a flash evaporation unit and a product separation unit, the reaction unit is provided with a first inlet, a first outlet and a second outlet, the first outlet of the reaction unit is communicated with the inlet of the sleeve heat exchange unit, the outlet of the sleeve heat exchange unit is communicated with the first inlet of the reaction unit, and the flash evaporation unit is communicated with the product separation unit. And a second outlet of the reaction unit is sequentially communicated with the flash evaporation unit and the product separation unit. The alpha-olefin production system provided by the utility model is used for reducing the adhesion phenomenon of the byproduct polymer to the reactor wall, the heat exchanger wall or other parts in the production process, and the continuous operation period of equipment is prolonged.

Description

Technical Field

[0001] The present disclosure relates to the technical field of α-olefin synthesis, and particularly to a production system for α-olefins. Background Art

[0002] α-olefins are an important type of terminal olefin products and have very wide applications in fields such as polyolefin comonomers, plasticizers, synthetic intermediates for surfactants, synthetic base oils for high-grade lubricants, and lubricant additives.

[0003] Currently, the main process for producing higher α-olefins such as 1-hexene and 1-octene is ethylene oligomerization. In the oligomerization reaction, polyethylene oligomers (such as polyethylene wax) are prone to deposit and adsorb on the surface of some metal vessel walls, and the active centers adsorb on the surface of these oligomers and continue to grow polyethylene on the surface of the oligomers. Over time, the polymers generated by oligomerization accumulate and adhere to the surfaces of the reactor walls, heat exchangers, agitator blades, or the impellers of the circulation pumps, making the heat continuously accumulate on the metal vessel walls and difficult to remove. Coupled with the adsorption of the catalyst by the polymers, it further causes the concentration of active centers on the metal vessel walls to be too high, resulting in more and more polymers generated by the reaction piling up, ultimately affecting heat and mass transfer and making it difficult for the equipment to operate normally, significantly reducing the continuous operation cycle of the oligomerization reaction. Summary of the Utility Model

[0004] In view of the above problems, the present disclosure is proposed. The present disclosure provides a production system for α-olefins, which reduces the adhesion of by-product polymers in the production process to the reactor walls, heat exchanger walls, or other parts, and improves the continuous operation cycle of the equipment.

[0005] According to one aspect of the present disclosure, there is provided a production system for α-olefins, including: a reaction unit, a double-pipe heat exchange unit, a flash evaporation unit, and a product separation unit. The reaction unit has a first inlet, a first outlet, and a second outlet. The first outlet of the reaction unit is communicated with the inlet of the double-pipe heat exchange unit, the outlet of the double-pipe heat exchange unit is communicated with the first inlet of the reaction unit, and the second outlet of the reaction unit is sequentially communicated with the flash evaporation unit and the product separation unit.

[0006] Compared with the prior art, in the production system of α-olefins provided by the present disclosure, it includes a reaction unit, a double-pipe heat exchange unit, a flash unit, and a product separation unit. Among them, the reaction unit has a first inlet, a first outlet, and a second outlet. The first outlet of the reaction unit is communicated with the inlet of the double-pipe heat exchange unit, and the outlet of the double-pipe heat exchange unit is communicated with the first inlet of the reaction unit. Therefore, the heat exchange unit can heat-exchange and condense the reaction liquid coming from the reaction unit, and then transport it into the reaction unit through the first inlet of the reaction unit. By adjusting the flow rate and temperature of the cooling water in the double-pipe heat exchange unit, the purpose of controlling the temperature inside the reaction unit can be achieved, so that the reaction temperature in the reaction unit can be kept stable, effectively suppressing the adhesion phenomenon of by-product polymers generated during the reaction to the reactor wall, heat exchanger wall or other parts, and then greatly improving the continuous operation period of the equipment.

[0007] On this basis, since the second outlet of the reaction unit is successively communicated with the flash unit and the product separation unit, therefore, the reaction liquid coming from the reaction unit can first enter the flash unit for flashing to remove impurities, and then enter the product separation unit for separation. BRIEF DESCRIPTION OF THE DRAWINGS

[0008] By describing the embodiments of the present disclosure in more detail in conjunction with the accompanying drawings, the above and other objects, features, and advantages of the present disclosure will become more obvious. The accompanying drawings are used to provide a further understanding of the embodiments of the present disclosure, and constitute a part of the specification. Together with the embodiments of the present disclosure, they are used to explain the present disclosure and do not constitute a limitation to the present disclosure. In the accompanying drawings, the same reference numerals generally represent the same components or steps.

[0009] Figure 1 is the process flow diagram of the production system of α-olefins provided by the embodiments of the present disclosure.

[0010] REFERENCE SIGNS

[0011] 100 - reaction unit, 100a - first inlet, 100b - first outlet, 100c - second outlet, 100d - second inlet, 100e - third inlet, 200 - double-pipe heat exchange unit, 300 - flash unit, 400 - product separation unit, 410 - 1-hexene rectification unit, 420 - solvent recovery unit; 430 - 1-octene rectification unit, 500 - mixing unit, 600 - catalyst feeding unit, 610 - catalyst feeding pipe, 620 - cocatalyst feeding pipe, 630 - mixing pipe, 700 - storage unit; 800 - filtering unit, A - first feeding pipe, B - second feeding pipe, C - third feeding pipe. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0012] To make the objectives, technical solutions, and advantages of the present disclosure more apparent, exemplary embodiments according to the present disclosure will be described in detail below with reference to the accompanying drawings. Apparently, the described embodiments are only a part of the embodiments of the present disclosure, rather than all embodiments of the present disclosure. It should be understood that the present disclosure is not limited by the exemplary embodiments described herein.

[0013] 1-Hexene and 1-octene are important comonomers for producing high-performance high-density polyethylene (HDPE) and linear low-density polyethylene (LLDPE), and are also important raw materials for producing fine chemicals such as spices, dyes, plasticizers, surfactants, and fatty alcohols. Currently, the main process for producing higher α-olefins such as 1-hexene and 1-octene is ethylene oligomerization. However, the biggest difficulty affecting the industrial application of ethylene oligomerization is the accumulation of polymers, which affects the continuous operation time of the device.

[0014] Polyethylene oligomers (such as polyethylene wax) generated in the oligomerization reaction are prone to deposit and adsorb on the surface of some metal walls, and the active centers are adsorbed on the surface of these oligomers, and polyethylene continues to grow on the surface of the oligomers. Over time, the polymers generated by oligomerization accumulate and adhere to the walls of the reactor, heat exchangers, agitator paddles, or the surfaces of the impellers of the circulation pumps, making the heat continuously accumulate on the metal walls and difficult to remove. Coupled with the adsorption of the catalyst by the polymers, it further causes the concentration of active centers on the metal walls to be too high, resulting in more and more polymers generated by the reaction accumulating. Eventually, it affects heat and mass transfer, making it difficult for the equipment to operate normally and significantly reducing the continuous operation cycle of the oligomerization reaction.

[0015] To address the above problems, the embodiments of the present disclosure provide a production system for α-olefins to reduce the adhesion of by-product polymers during the production process to the reactor walls, heat exchanger walls, or other parts, improve the continuous operation cycle of the equipment, and solve the problem in the prior art that polyethylene oligomers generated during the production of α-olefins by oligomerization are prone to accumulate on the tube wall surface of the reaction system, affecting heat and mass transfer and making it difficult for the equipment to operate normally.

[0016] Figure 1 The process flow diagram of the production system for α-olefins provided by the embodiments of the present disclosure is shown. As Figure 1 shown, the production system for α-olefins of the embodiments of the present disclosure includes: a reaction unit 100, a double-pipe heat exchange unit 200, a flash evaporation unit 300, and a product separation unit 400. The reaction unit 100 has a first inlet 100a, a first outlet 100b, and a second outlet 100c. The first outlet 100b of the reaction unit 100 is communicated with the inlet of the double-pipe heat exchange unit 200, the outlet of the double-pipe heat exchange unit 200 is communicated with the first inlet 100a of the reaction unit 100, and the second outlet 100c of the reaction unit 100 is sequentially communicated with the flash evaporation unit 300 and the product separation unit 400.

[0017] It is understandable that the above reaction unit 100 can be a reaction kettle for carrying out ethylene oligomerization reaction. The first outlet 100b of the reaction unit 100 can be arranged at the bottom of the reaction unit 100. The second outlet 100c of the reaction unit is above the 70% liquid level of the reaction unit 100, and the height of the second outlet 100c is greater than the height of the first inlet 100a. The second outlet 100c is an overflow port.

[0018] In specific implementation, first, the ethylene oligomerization reaction can be carried out by using the reaction unit 100. After reacting for a certain time, the reaction liquid is discharged from the first outlet 100b of the reaction unit 100, and then heat exchange and condensation are carried out by using the double-pipe heat exchange unit 200. The heat-exchanged reaction liquid is then transported into the reaction unit 100 through the first inlet 100a of the reaction unit 100. Therefore, by adjusting the flow rate and temperature of the cooling water in the double-pipe heat exchange unit 200, the purpose of internal temperature control of the reaction unit can be achieved, so that the reaction temperature in the reaction unit can be kept stable, effectively inhibiting the adhesion phenomenon of by-product polymers generated during the reaction to the reactor wall, heat exchanger wall or other parts, and thus greatly improving the continuous operation period of the equipment.

[0019] On this basis, since the second outlet 100c of the reaction unit 100 is sequentially connected to the flash evaporation unit 300 and the product separation unit 400, the reaction liquid coming from the reaction unit 100 can first enter the flash evaporation unit 300 for flash evaporation to remove impurities, and then enter the product separation unit 400 for separation.

[0020] Exemplarily, the above double-pipe heat exchange unit 200 includes an inner pipe, an outer pipe sleeved outside the inner pipe and a circulation pump. Among them, the inner pipe is used for the circulation of the reaction liquid, the outer pipe is used for the circulation of the cooling water, and the circulation pump is used for transporting the cooling water into the outer pipe. When the reaction liquid flows through the inner pipe, the cooling water in the outer pipe can carry out condensation heat exchange on the reaction liquid. The length of the double-pipe heat exchange unit 200 is 10 - 12 meters, the pipe diameter is DN80, folded into three folds, and from the first outlet 100b at the bottom of the reaction unit 100 to the first inlet 100a near the lower part of 100c. The water temperature of the circulating cooling water is set at 30°C - 35°C, which can reduce the temperature difference between the circulating water and the reaction.

[0021] For example, the above reaction unit is provided with a stirrer. The stirrer includes multiple layers of stirring paddles for promoting the occurrence of the reaction. The stirring paddles are propeller-type stirring paddles, and the advancing directions of the stirring paddles all face the bottom of the reaction unit 100. The ratio of the radial length L of the propeller-type stirring paddle to the diameter D of the reaction kettle is L / D = 0.1 - 0.4, preferably 0.2 - 0.4, and exemplarily 0.1, 0.15, 0.2, 0.25, 0.3, 0.4.

[0022] In one example, the above-mentioned stirrer further includes a driving part for adjusting the stirring speed of the stirrer. For example, the driving part is a motor, and the driving part can be located at the top of the reaction unit.

[0023] The outlet position of the above-mentioned casing heat exchange unit 200 is not higher than the lowermost stirring paddle in the reaction unit, such as the bottom stirring paddle, and is preferably flush with the lowermost stirring paddle, such as the bottom stirring paddle. The first inlet 100a of the reaction unit 100 is not higher than the uppermost stirring paddle, such as the top stirring paddle.

[0024] In one example, a heating jacket is further provided outside the reaction unit 100 of the embodiments of the present disclosure for heating the reaction unit 100.

[0025] In an alternative manner, the production system of the embodiments of the present disclosure further includes a mixing unit 500 and a catalyst feeding unit 600. The reaction unit 100 further has a second inlet 100d and a third inlet 100e. The outlet of the mixing unit 500 is communicated with the second inlet 100d of the reaction unit 100, and the outlet of the catalyst feeding unit 600 is communicated with the third inlet 100e of the reaction unit 100.

[0026] During specific implementation, the above-mentioned mixing unit 500 can be used to transport raw materials into the reaction unit 100, and the above-mentioned catalyst feeding unit 600 can be used to transport the catalyst into the reaction unit 100. Then, under the action of the catalyst, the raw materials undergo an ethylene oligomerization reaction in the reaction unit 100.

[0027] Exemplarily, the gas outlet of the flash evaporation unit 300 of the embodiments of the present disclosure is communicated with the inlet of the mixing unit 500. Therefore, when the reaction liquid enters the flash evaporation unit 300, the flash evaporation unit can flash out the unreacted ethylene in the reaction liquid, and then transport it to the mixing unit 500 through the gas outlet. Therefore, the unreacted ethylene can enter the mixing unit 500 for recycling, saving raw materials, avoiding waste, and reducing the complexity of post-treatment.

[0028] In an alternative manner, the production system of the embodiments of the present disclosure further includes a first feed pipe A, a second feed pipe B, and a third feed pipe C. The first feed pipe A, the second feed pipe B, and the third feed pipe C are respectively communicated with the inlet of the mixing unit 500. The first feed pipe A is used to transport ethylene to the mixing unit 500, the second feed pipe B is used to transport hydrogen to the mixing unit 500, and the third feed pipe C is used to transport a reaction solvent to the mixing unit 500.

[0029] In specific implementation, ethylene, hydrogen, and reaction solvent can be simultaneously transported into the mixing unit 500 through the above-mentioned first feed pipe A, second feed pipe B, and third feed pipe C for mixing. Among them, the oxygen content of ethylene is greater than 5 ppm, and a certain oxygen content can inhibit the generation of polyethylene oligomers in the reaction.

[0030] In practical applications, the above-mentioned reaction solvent can be a solvent of linear alkanes with more than C7, such as heptane. On the one hand, based on the principle of similar solubility, the generated polyethylene oligomers can be dissolved in the solvent, achieving the elimination of the problem of oligomer sticking to the kettle. On the other hand, heptane can dissolve the side reaction product PE relatively quickly, avoiding the adhesion of PE to parts such as the inner wall of the reactor and the stirring paddle, and avoiding the re-polymerization at the adhered PE parts. Furthermore, the generation amount of the polymer PE is significantly reduced, and almost no polymer can be seen in the kettle. Moreover, by using these solvents with boiling points significantly higher than those of 1-hexene and 1-octene, it is easier to separate 1-hexene and 1-octene, and the reaction solvent is directly recycled after separating 1-hexene and 1-octene, improving the continuous operation time of the device, greatly enhancing the production efficiency, and having high economic added value.

[0031] In an implementable manner, the catalyst feeding unit 600 of the present disclosure includes a catalyst feed pipe 610, a co-catalyst feed pipe 620, and a mixing pipe 630. The outlets of the catalyst feed pipe 610 and the co-catalyst feed pipe 620 are respectively communicated with the inlet of the mixing pipe 630, and the outlet of the mixing pipe 630 is communicated with the third inlet 100e of the reaction unit 100.

[0032] In specific implementation, the main catalyst can be transported into the mixing pipe 630 by using the above-mentioned catalyst feed pipe 610, and the co-catalyst can be transported into the mixing pipe 630 by using the co-catalyst feed pipe 620 for mixing.

[0033] In practical applications, the above-mentioned mixing pipe 630 can be a tubular static mixer, such as an SV static mixer or an SX type static mixer, or other tubular mixers with a mixing function structure inside.

[0034] In an example, a configured catalyst solution and co-catalyst solution can be input into the mixing pipe 630 by using a pump. The catalyst solution and the co-catalyst solution are mixed and activated in the mixing pipe 630, and an activated ethylene oligomerization catalyst can be prepared, and then enter the reaction unit 100 for reaction. The pump can be selected from a diaphragm pump, a plunger pump, or a screw pump.

[0035] In an alternative manner, the production system of the present disclosure further includes a storage unit 700. The outlet of the flash unit 300 is communicated with the inlet of the storage unit 700, and the inlet of the storage unit 700 is communicated with the inlet of the product separation unit 400.

[0036] In specific implementation, the flash evaporation unit described above can be used to transport the reaction liquid after flash evaporation into the storage unit 700 for storage, then cooled to room temperature, and then transported into the product separation unit 400 for separation.

[0037] In one example, the product separation unit 400 of the embodiments of the present disclosure includes a 1-hexene rectification unit 410, a solvent recovery unit 420, and a 1-octene rectification unit 430. The 1-hexene rectification unit 410, the solvent recovery unit 420, and the 1-octene rectification unit 430 are connected in sequence, and the outlet of the storage unit 700 is connected to the inlet of the 1-hexene rectification unit 410.

[0038] In specific implementation, the reaction liquid coming out of the storage unit 700 can enter the 1-hexene rectification unit 410 to separate 1-hexene, then enter the solvent recovery unit 420 to recover the reaction solvent, and then enter the 1-octene rectification unit 430 to recover 1-octene, thereby completing the production process of α-olefins.

[0039] Exemplarily, the production system of the embodiments of the present disclosure further includes a filtration unit 800. The outlet of the storage unit 700 is connected to the inlet of the filtration unit 800, and the liquid outlet of the filtration unit 800 is connected to the inlet of the product separation unit 400.

[0040] In specific implementation, the storage unit 700 can be used to transport the reaction liquid into the filtration unit 800 for filtration, and the filtrate enters the product separation unit 400 for separation. The filtration unit 800 can filter out the catalyst in the reaction liquid, thus facilitating subsequent product separation.

[0041] It can be understood that the above filtration unit can be a filter. Specifically, the filter can be a sleeve filter. The filtrate flows out from the side of the sleeve, and the polyethylene oligomer flows out from the lower part of the sleeve. Since the oligomers generated by this process are very few, usually not exceeding 0.1%, it is not necessary to clean the filter frequently. It only needs to seal the lower part of the filtration port with a flange and process it regularly.

[0042] The height of the above-mentioned cylindrical filter is 0.1 - 0.3D, preferably 0.2D. The aperture of the filter screen of the filter can be 5μm - 20μm, preferably 5μm - 10μm.

[0043] Exemplarily, there are also multiple baffle plates inside the reaction unit 100 of the embodiments of the present disclosure. The multiple baffle plates are installed on the inner wall of the reaction unit 100. The multiple baffle plates can be installed on the inner wall of the reaction unit corresponding to the stirring paddle at uniform intervals. The baffle plate can be an arc-shaped flat plate. For example, the arc-shaped flat plate can be a semi-circular flat plate. Further, the long side of the baffle plate can be welded and fixed to the inner wall of the reactor body, being integrated with the inner wall of the body.

[0044] In an alternative embodiment, the production system of the present disclosure may further include a control system. Preferably, the control system may be a DCS control system. Specifically, the control system may be electrically connected or signal-connected to the reaction unit, the jacket heat exchange unit, and the pump to achieve ethylene feed flow control and interlock temperature control of the cooling water flow in the outer tube and the internal temperature of the reaction unit.

[0045] Exemplarily, the embodiments of the present disclosure can control and adjust the temperature and flow rate of the cooling water through a DCS controller to meet the requirements for reactor temperature control during the polymerization reaction process. Specifically, the control system is used to control the internal temperature of the reaction unit, the circulating flow rate of the reaction slurry in the inner tube of the jacket heat exchange unit, and the circulating flow rate of the cooling water in the outer tube. The temperature is controlled by interlocking the cooling water flow rate in the outer tube and the internal temperature of the reactor body, so that the cooling water flow rate in the outer tube can be adjusted according to the change in the internal temperature of the reaction unit.

[0046] In practical applications, the purpose of internal temperature control of the reaction unit 100 can be achieved by adjusting the cooling water flow rate in the outer tube. And when the heat generated by the reaction is the same, if it is necessary to make the internal temperature of the reaction unit 100 higher, the cooling water flow rate can be reduced. On the contrary, if it is necessary to make the internal temperature of the reactor body lower, the circulating cooling water flow rate can be increased.

[0047] Example 1

[0048] Taking a 3-cubic-meter high-pressure reactor as an example, the ethylene oligomerization reaction is carried out as follows:

[0049] 1. Equipment setup: The length of the solution external circulation jacket heat exchanger of the reactor is 10 meters, the pipe diameter is DN80, folded into three folds, entering from the bottom of the reactor near the lower part of the overflow port, and the overflow port is set above 70% liquid level of the reactor. The circulating water temperature is set at 30 °C; the pipe mixer is set for 45 seconds of mixing.

[0050] 2. Raw material treatment: The oxygen content of the solvent heptane is less than 2 ppm and the water content is less than 2 ppm after deoxygenation and dehydration pretreatment; ethylene only needs dehydration treatment without deoxygenation, and the oxygen content of ethylene is 5 ppm.

[0051] 3. Configure a chromium-based catalyst.

[0052] 4. Configure the cocatalyst modified methylaluminoxane (MMAO 3A).

[0053] 5. Oligomerization reaction: First, the solvent heptane is initially filled to 70% of the liquid level in the reaction unit 100. Then, after ethylene, hydrogen, and the solvent are mixed in the mixing unit 500, the mixing unit 500 is controlled at a temperature of 5°C. The chromium-based catalyst is configured at a concentration of 0.06 mol, and the cocatalyst MMAO 3A (10 wt.%) is at Al / Cr = 500. After being mixed through the mixing pipe 630, it is introduced into the reaction unit 100. After continuous reaction, the solvent feed rate is 200 kg / hr, and the ethylene feed rate is 180 kg / hr. The feed enters the compressor inlet and then enters the double-pipe heat exchange unit 200. And through the double-pipe heat exchange unit 200, an external solution circulation is carried out to raise the pressure of the reaction unit 100 to 6 MPa. The reaction temperature is controlled at 60°C. After 30 minutes of reaction, it is discharged through the first inlet (overflow port) under heat preservation. The reaction liquid is quenched by a quenching agent and then enters the flash evaporation unit 300 to recover unreacted ethylene. After flash evaporation, the reaction liquid enters the storage unit 700 and is cooled to room temperature. The polyethylene solid is recovered through the filtration unit 800 at the lower part of the storage unit 700; the liquid phase of the storage unit 700 enters the 1-hexene rectification unit 410, the solvent recovery unit 420, and the 1-octene rectification unit 430 to obtain purified 1-hexene product and 1-octene product. The residue in the bottom of the 1-octene rectification tower 11 is C10+α olefins, and the C10+α olefins are recovered. After 72 hours of operation, it is checked that the inside of the kettle and the external circulation pipeline are very clean and there is no obvious solid.

[0054] As described above, with reference to the drawings, the production system of α-olefins according to the embodiments of the present disclosure is described. Through the heat exchange unit, the reaction liquid coming from the reaction unit can be heat-exchanged and condensed, and then transported into the reaction unit through the first inlet of the reaction unit. By adjusting the cooling water flow rate and temperature in the double-pipe heat exchange unit, the purpose of controlling the temperature inside the reaction unit is achieved, so that the reaction temperature inside the reaction unit can be kept stable, effectively suppressing the adhesion phenomenon of by-product polymers generated during the reaction to the reactor wall, heat exchanger wall or other parts, and thus greatly improving the continuous operation period of the equipment.

[0055] The basic principle of the present disclosure has been described above in combination with specific embodiments. However, it should be noted that the advantages, advantages, effects, etc. mentioned in the present disclosure are only examples and not limitations. It cannot be considered that these advantages, advantages, effects, etc. are essential for each embodiment of the present disclosure. In addition, the above-mentioned specific details are only for the purposes of illustration and easy understanding, rather than limitations. The above details do not limit the present disclosure to necessarily adopt the above specific details to implement.

[0056] The block diagrams of devices, apparatuses, equipment, and systems involved in this disclosure are only illustrative examples and are not intended to require or imply that they must be connected, arranged, and configured in the manner shown in the block diagrams. As those skilled in the art will recognize, these devices, apparatuses, equipment, and systems can be connected, arranged, and configured in any way. Words such as "including", "comprising", "having", etc. are open-ended terms, meaning "including but not limited to", and can be used interchangeably with each other. The words "or" and "and" used herein refer to the phrase "and / or", and can be used interchangeably with it, unless the context clearly indicates otherwise. The word "such as" used herein refers to the phrase "such as but not limited to", and can be used interchangeably with it.

[0057] In addition, as used herein, the "or" used in the listing of items starting with "at least one" indicates a disjunctive listing. So, for example, the listing of "at least one of A, B, or C" means A or B or C, or AB or AC or BC, or ABC (i.e., A and B and C). Further, the term "exemplary" does not mean that the examples described are preferred or better than other examples.

[0058] It should also be noted that in the systems and methods of this disclosure, each component or each step can be decomposed and / or recombined. These decompositions and / or recombinations should be regarded as equivalent solutions of this disclosure.

[0059] Various changes, substitutions, and alterations to the technologies described herein can be made without departing from the teachings defined by the appended claims. Moreover, the scope of the claims of this disclosure is not limited to the specific aspects of the processes, machines, manufactures, compositions of events, means, methods, and acts described above. Current or later-developed processes, machines, manufactures, compositions of events, means, methods, or acts that perform substantially the same function or achieve substantially the same result as the corresponding aspects described herein can be utilized. Thus, the appended claims include such processes, machines, manufactures, compositions of events, means, methods, or acts within their scope.

[0060] The above description of the disclosed aspects is provided to enable any person skilled in the art to make or use this disclosure. Various modifications to these aspects will be readily apparent to those skilled in the art, and the general principles defined herein can be applied to other aspects without departing from the scope of this disclosure. Therefore, this disclosure is not intended to be limited to the aspects shown herein, but rather to the broadest scope consistent with the principles and novel features disclosed herein.

[0061] The foregoing description has been presented for purposes of illustration and description. In addition, this description is not intended to limit embodiments of the present disclosure to the form disclosed herein. Although several example aspects and embodiments have been discussed above, those skilled in the art will recognize some of their variations, modifications, alterations, additions, and subcombinations.

Claims

1. A system for producing α-olefins, characterized in that: include: A reaction unit, a shell and tube heat exchange unit, a flash unit and a product separation unit, wherein the reaction unit has a first inlet, a first outlet and a second outlet, the first outlet of the reaction unit is connected to the inlet of the shell and tube heat exchange unit, the outlet of the shell and tube heat exchange unit is connected to the first inlet of the reaction unit, and the second outlet of the reaction unit is connected to the flash unit and the product separation unit in sequence.

2. The α-olefin production system according to claim 1, characterized in that: The second outlet of the reaction unit is located above 70% of the liquid level of the reaction unit, and the height of the second outlet is greater than the height of the first inlet.

3. The α-olefin production system according to claim 1, characterized in that: The production system further comprises a mixing unit and a catalyst feeding unit, the reaction unit further comprises a second inlet and a third inlet, the outlet of the mixing unit is connected to the second inlet of the reaction unit, and the outlet of the catalyst feeding unit is connected to the third inlet of the reaction unit.

4. The α-olefin production system according to claim 3, characterized in that: The gas outlet of the flash unit is communicated with the inlet of the mixing unit.

5. The α-olefin production system according to claim 3, characterized in that: The production system also includes a first feed pipe, a second feed pipe and a third feed pipe, wherein the first feed pipe, the second feed pipe and the third feed pipe are respectively connected to the inlet of the mixing unit, the first feed pipe is used to transport ethylene to the mixing unit, the second feed pipe is used to transport hydrogen to the mixing unit, and the third feed pipe is used to transport a reaction solvent to the mixing unit.

6. The α-olefin production system according to claim 3, characterized in that: The catalyst feed unit comprises a catalyst feed pipe, a co-catalyst feed pipe and a mixing pipe, the outlets of the catalyst feed pipe and the co-catalyst feed pipe are respectively connected to the inlet of the mixing pipe, and the outlet of the mixing pipe is connected to the third inlet of the reaction unit.

7. The α-olefin production system according to claim 1, characterized in that: The production system further includes a storage unit, the outlet of the flash unit is in communication with the inlet of the storage unit, and the inlet of the storage unit is in communication with the inlet of the product separation unit.

8. The α-olefin production system according to claim 7, characterized in that: The product separation unit comprises a 1-hexene distillation unit, a solvent recovery unit and a 1-octene distillation unit, which are connected in sequence, and the outlet of the storage unit is connected to the inlet of the 1-hexene distillation unit.

9. The α-olefin production system according to claim 7, characterized in that: The production system further includes a filtration unit, the outlet of the storage unit is communicated with the inlet of the filtration unit, and the liquid outlet of the filtration unit is communicated with the inlet of the product separation unit.

10. The α-olefin production system according to any one of claims 1 to 9, characterized in that: The reaction unit is further provided with a plurality of guide plates inside, and the plurality of guide plates are installed on the inner wall of the reaction unit.

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