CN210855896U - Production system for synthesizing 1-octene and 1-hexene through ethylene oligomerization - Google Patents
Production system for synthesizing 1-octene and 1-hexene through ethylene oligomerization Download PDFInfo
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- CN210855896U CN210855896U CN201921865342.4U CN201921865342U CN210855896U CN 210855896 U CN210855896 U CN 210855896U CN 201921865342 U CN201921865342 U CN 201921865342U CN 210855896 U CN210855896 U CN 210855896U
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Abstract
The utility model provides a production system for synthesizing 1-octene and 1-hexene by ethylene oligomerization, which comprises a raw material compression unit, a reaction polymerization unit, a reaction termination unit and a product separation unit which are connected in sequence; the product separation unit comprises a 1-hexene separation device and a 1-octene separation device which are sequentially connected. The utility model provides a production system has realized producing two kinds of different products of 1-octene and 1-hexene in the different workshop sections under same flow, has not only realized the high-efficient separation of reaction product, saves investment greatly, reduces the energy consumption, can adjust the selectivity of product moreover through the addition and the ratio of control catalyst.
Description
Technical Field
The utility model belongs to the technical field of 1-octene and 1-hexene preparation, a production system of 1-octene and 1-hexene is related to, especially relate to a production system of ethylene oligomerization synthesis 1-octene and 1-hexene.
Background
With the rapid development of polyethylene industry, 1-octene and 1-hexene are increasingly demanded as important comonomers and important chemical raw materials for synthesizing high-performance polyethylene.
The 1-octene is an important organic chemical raw material and chemical intermediate, is mainly used as a comonomer of Linear Low Density Polyethylene (LLDPE), can also be used for producing plasticizers, detergents, synthetic oil, surfactants and the like, is particularly suitable for producing PE-RT (heat-resistant polyethylene) and POE (polyolefin elastomer), and a copolymerization product has the advantages of high toughness, high tear resistance, high temperature and pressure resistance, convenience and reliability in connection.
1-hexene is a main comonomer for synthesizing Linear Low Density Polyethylene (LLDPE) and High Density Polyethylene (HDPE) with high added value and high performance, and compared with a butene copolymerization product, the 1-hexene copolymerization product has the advantages of high tensile strength, strong impact resistance and tear resistance and the like, and is widely applied to industries of agriculture, packaging, building materials and the like.
At present, the domestic demand of 1-octene and 1-hexene is about 85 ten thousand tons/year, and the product is basically in a complete import state. With the increasing demand for quality, the demand for 1-octene and 1-hexene in particular will increase. Foreign related process technologies are in monopoly and secretly kept from the domestic state, which is in the experimental research stage. The development of a process technology for synthesizing 1-octene and 1-hexene is urgent and very important.
Currently, the main processes for producing higher α olefins such as 1-hexene, 1-octene, etc. are ethylene oligomerization processes such as:
CN106588551A discloses a method for separating 1-hexene from an ethylene oligomerization product, which comprises the following steps: introducing the ethylene oligomerization product I into a flash tank for flash evaporation, and feeding a liquid-phase discharge II flowing out of the flash tank into a light component removal tower; introducing a liquid phase discharge material III flowing out of the light component removal tower into a carbon six separation tower to obtain a 1-hexene product; carrying out gas-liquid separation on a gas-phase discharge IV flowing out of the flash tank through condensation, and introducing the obtained gas phase V into a carbon four-separation tower; gas-liquid separation is carried out on a gas-phase discharge VI flowing out of the light component removal tower through condensation, and an obtained gas phase VII is introduced into a carbon four-separation tower; rectifying in a carbon four separation tower to obtain 1-hexene isomer at the bottom of the tower.
CN102464545A discloses a method for preparing 1-octene by ethylene oligomerization, which comprises the following steps: (1) after premixing part of raw material ethylene gas and a solvent in a premixer, mixing the premixed raw material ethylene gas with a catalytic system a + b component, a component c and a component d, and then entering a reactor through a gas distributor, wherein the other part of raw material ethylene gas directly enters the reactor; (2) the reaction liquid of the reactor flows out to the overflow groove from the middle upper part, the catalyst terminator is added into the overflow groove, and then the reaction product enters the separation device.
CN106588551A discloses a method for preparing 1-hexene in the presence of an ethylene oligomerization catalyst system, which specifically comprises the following steps: (1) after premixing a part of raw material ethylene and a solvent in a premixer, respectively mixing the raw material ethylene and the solvent with a chromide (a) of a catalyst for preparing 1-hexene by ethylene oligomerization, a pyrrole derivative (b), an alkyl aluminum (c) and an improver (d), and then feeding the mixture into a reactor with a stirrer through a gas distributor; (2) the other part of the ethylene gas directly enters the reactor; (3) the reaction liquid of the reactor flows out to the overflow groove from the middle part, the catalyst terminator is added in the overflow groove, and then the reaction product enters the separation device.
However, in summary, the currently known ethylene oligomerization reaction system can only produce one product, and cannot realize the co-production of 1-octene and 1-hexene, so at least two sets of equipment are required for separately producing 1-octene and 1-hexene, and in order to simplify the production flow and reduce the equipment investment cost, it is necessary to design a production system for realizing the co-production of 1-octene and 1-hexene.
SUMMERY OF THE UTILITY MODEL
The utility model aims to the deficiency that prior art exists, the utility model aims to provide an ethylene oligomerization synthesis 1-octene and 1-hexene's production system, the utility model discloses an ethylene oligomerization synthesis 1-octene and 1-hexene realizes synthesizing 1-octene, 1-hexene's complete set flow through raw materials compression unit, reaction polymerization unit, termination reaction unit and result separation unit. The complete equipment realizes the production of two different products of 1-octene and 1-hexene in different working sections under the same flow, not only realizes the high-efficiency separation of reaction products, greatly saves the investment and reduces the energy consumption, but also can adjust the proportion of the two products according to the production requirements.
To achieve the purpose, the utility model adopts the following technical proposal:
in a first aspect, the utility model provides a production system for 1-octene and 1-hexene are synthesized to ethylene oligomerization, production system including raw materials compression unit, reaction polymerization unit, termination reaction unit and the product separation unit that connects gradually.
The product separation unit comprises a 1-hexene separation device and a 1-octene separation device which are sequentially connected.
The utility model discloses an ethylene oligomerization synthesis 1-octene and 1-hexene realizes synthesizing 1-octene, 1-hexene's complete set flow through raw materials compression unit, reaction polymerization unit, termination reaction unit and product separation unit. The complete equipment realizes the production of two different products of 1-octene and 1-hexene in different working sections under the same flow, not only realizes the high-efficiency separation of reaction products, greatly saves the investment and reduces the energy consumption, but also can adjust the selectivity of the products (1-octene and 1-hexene) by controlling the adding amount and the proportion of the catalyst.
It should be noted that, in the present invention, the 1-hexene separation device and the 1-octene separation device are olefin separation devices known in the art, and mainly include a rectification column device, a vacuum pumping system and other accessories, and the structures and functions thereof are well known to those skilled in the art and will not be described herein again.
As a preferred technical scheme of the utility model, raw materials compression unit include compressor arrangement, compressor arrangement be used for compressing the ethylene raw materials.
The utility model discloses in, still be provided with raw materials in compressor arrangement anterior segment process and divide liquid device for carry out gas-liquid separation to the raw materials, the gaseous ethylene that obtains after the separation gets into compressor arrangement, because there is a small amount of liquid in the raw materials, need separate away the liquid wherein before getting into compressor arrangement in advance, this is the conventional operation that compressor arrangement was advanced to the raw materials in this field.
As a preferred technical scheme of the utility model, the reaction polymerization unit includes reaction unit.
The upper part, the middle part and the lower part of the reaction device are provided with a catalyst injection port and a cocatalyst injection port.
The reaction device is a stirred tank reactor.
The utility model discloses in, the reaction polymerization unit still includes catalyst configuration and injection apparatus, catalyst configuration and injection apparatus dispose the catalyst earlier, pour into to reaction unit through the catalyst injection pump afterwards.
As an optimal technical scheme, the connecting pipeline between compressor arrangement and the reaction unit on external solvent feed line, the ethylene raw materials get into reaction unit through the solvent mixture that lets in compressor arrangement compression back and the solvent feed line.
As an optimal technical scheme, the inside inner coil that sets up of reaction unit, inner coil be helical structure, let in cooling medium to the inner coil inside and cool down to reaction unit.
As an optimized technical proposal, the shell outside of the reaction device is provided with a jacket, and the cooling medium is introduced into the jacket to cool the inside of the reaction device.
As a preferred technical scheme, reaction polymerization unit still remove the heat device including the circulation, the circulation remove the heat device and include circulation line, circulation line's one end insert reaction unit's bottom circulation export, circulation line's the other end inserts reaction unit's top circulation entry, along reaction liquid flow direction, circulation line on set gradually circulating pump and cooling device.
In fact, the utility model provides three different heat removal schemes, one of which is to cool the interior of the reaction device by introducing a cooling medium into an inner coil pipe arranged in the interior of the reaction device; secondly, cooling the interior of the reaction device by introducing a cooling medium into a jacket coated on the outer side of the reaction device; and thirdly, controlling the reaction temperature by circularly cooling the high-temperature reaction product in the reaction device through a circulating pipeline through a circulating heat removal device. Those skilled in the art need a heat removal scheme in which one or more of them are freely selected depending on the reaction temperature in the reaction apparatus.
The heat of polymerization reaction in the reaction device is timely removed, so that the equilibrium and stability of the reaction temperature are ensured, and the wall sticking phenomenon of polymerization byproducts in subsequent equipment and pipelines is favorably reduced.
As a preferred technical proposal of the utility model, the termination reaction unit comprises a termination reaction device, and the ethylene oligomerization synthesis reaction is terminated by injecting a terminator into the termination reaction device.
The reaction terminating device is a stirred tank reactor.
The aspect ratio of the terminating reactor is 3.0 to 6.0, and may be, for example, 3.0, 3.1, 3.2, 3.3, 3.4, 3.5, 3.6, 3.7, 3.8, 3.9, 4.0, 4.1, 4.2, 4.3, 4.4, 4.5, 4.6, 4.7, 4.8, 4.9, 5.0, 5.1, 5.2, 5.3, 5.4, 5.5, 5.6, 5.7, 5.8, 5.9 or 6.0, but is not limited to the recited values, and other values not recited in the range of values are also applicable.
And the upper part and the middle part of the reaction terminating device are both provided with a terminating agent inlet.
The upper overflow port of the reaction device is connected with the liquid inlet of the reaction termination device through an overflow pipe, and the reaction product flows through the overflow pipe from the overflow port and enters the reaction termination device.
The overflow pipe is arranged obliquely downwards along the flow direction of the reaction products.
The angle between the overflow tube and the horizontal direction is 20 ° to 45 °, for example, 20 °, 21 °, 22 °, 23 °, 24 °, 25 °, 26 °, 27 °, 28 °, 29 °, 30 °, 31 °, 32 °, 33 °, 34 °, 35 °, 36 °, 37 °, 38 °, 39 °, 40 °, 41 °, 42 °, 43 °, 44 °, or 45 °, but is not limited to the values listed, and other values not listed in this range of values are also applicable.
It should be noted that, in the utility model, the technical personnel in the field guarantee the length setting of overflow pipe as short as possible according to equipment arrangement place size and system scale.
As an optimized technical scheme of the utility model, termination reaction unit and result separation unit between still be provided with ethylene desorption unit, ethylene desorption unit be arranged in desorption reaction product unreacted ethylene raw materials.
The ethylene removal unit comprises a flash evaporation device and a deethylenizer which are sequentially connected.
It should be noted that the flash distillation device and the deethylenizer defined in the present invention are conventional apparatuses in the art, and the structure and function thereof are well known to those skilled in the art, and the flash distillation device is a flash tank known in the art, and the deethylenizer is a deethylenizer known in the art.
The liquid outlet at the bottom of the reaction terminating device is connected with the liquid inlet of the flash evaporation device, the top collecting port of the flash evaporation device is externally connected with an ethylene gas collecting device, and the liquid outlet at the bottom of the flash evaporation device is connected with the liquid inlet of the ethylene removing device.
It should be noted that the ethylene gas collection device and the various collection devices hereinafter are various storage tanks known in the art, and the structure and function thereof are well known to those skilled in the art and will not be described herein again.
The top collecting port of the ethylene removing device is externally connected with an ethylene gas collecting device, and the bottom liquid outlet of the ethylene removing device is connected with the liquid inlet of the 1-hexene separating device.
As a preferred technical scheme of the utility model, the product separation unit still include solvent separator and accessory substance separator, along the product separation route, solvent separator set up between 1-hexene separator and 1-octene separator.
It should be noted that, in the present invention, the solvent separation device and the byproduct separation device are distillation column separation devices known in the art, and mainly include column equipment and other accessories, and the structure and function thereof are well known to those skilled in the art and will not be described herein again.
A top outlet of the 1-hexene separation device is connected with a 1-hexene collection device, and 1-hexene is collected from the top of the 1-hexene separation device and then enters the 1-hexene collection device; a liquid outlet at the bottom of the 1-hexene separation device is connected with a liquid inlet of the solvent separation device.
The top extraction port of the solvent separation device is divided into two paths, one path is connected to a solvent feeding pipeline, and the other path is connected with the liquid inlet of the byproduct separation device; and a liquid outlet at the bottom of the solvent separation device is connected with a liquid inlet of the 1-octene separation device.
A liquid outlet at the bottom of the byproduct separation device is connected with a solvent feeding pipeline, the separated solvent is extracted from the bottom of the tower and flows back to the solvent feeding pipeline, the byproduct separated by the byproduct separation device is discharged from the top of the tower, and the byproduct comprises methylcyclopentane.
And a production outlet at the top of the 1-octene separation device is connected with a 1-octene collection device, and 1-octene enters the 1-octene collection device after being produced from the top of the 1-octene separation device.
But not limited to, the recited values and other values not recited within the range of values are equally applicable.
Adopt the utility model provides a production system carries out the reaction of ethylene oligomerization synthesis 1-octene and 1-hexene, specifically includes following step:
(1) the method comprises the steps of boosting the pressure of raw material ethylene to 3.0-6.0 MPaG through a compression device, mixing the raw material ethylene with a solvent (one or a combination of at least two of cyclohexane, methyl cyclopentane or methyl cyclohexane), and then feeding the mixture into a reaction device, wherein the mass flow ratio of the solvent to the raw material is 2-6.
(2) Injecting catalyst and cocatalyst into the upper part, the middle part and the lower part of the reaction device, keeping the reaction temperature at 40-120 ℃, the reaction pressure at 3.0-6.0 MPaG and the reaction time at 0.8-1.5 h, and carrying out ethylene oligomerization while stirring. The reaction heat is rapidly and timely removed through an inner coil pipe, a jacket and a circulating heat removal device arranged outside the reaction device, and stable reaction conditions are ensured.
(3) Reaction products overflowing from the reaction device enter the reaction terminating device through the overflow pipe, the arrangement distance between the reaction device and the reaction terminating device is as short as possible, the inclination angle of the overflow pipe is 20-45 degrees, terminating agents are injected into the upper part and the middle part of the reaction terminating device, and the ethylene oligomerization reaction is rapidly terminated along with the stirring.
(4) The reaction product enters a flash evaporation device, the operation condition is controlled at 40-120 ℃, and the operation pressure is 1.6-2.5 MPaG. The ethylene gas extracted from the top of the flash evaporation device is introduced into an ethylene collecting device, and the discharge from the bottom of the flash evaporation device enters an ethylene removal device.
(5) The temperature of the top of the ethylene removing device is controlled to be 90-97 ℃, the operating pressure is controlled to be 1.2-1.4 MPaG, the temperature of the bottom of the ethylene removing device is controlled to be 200-210 ℃, and the operating pressure is controlled to be 1.25-1.45 MPaG. Leading ethylene gas extracted from the top of the ethylene removal device into an ethylene collecting device, and discharging from the bottom of the ethylene removal device into a 1-hexene separating device.
(6) The temperature of the top of the 1-hexene separation device is controlled between 100 ℃ and 105 ℃, and the operating pressure is controlled between 0.1MPaG and 0.15 MPaG. The temperature of the bottom of the 1-hexene separation device is controlled at 125-135 ℃, and the operating pressure is controlled at 0.15-0.20 MPaG. Introducing a 1-hexene product collected from the top of the 1-hexene separation device into a 1-hexene collecting device, and discharging the material from the bottom of the 1-hexene device to enter a solvent separation device.
(7) The temperature of the top of the solvent separation device is controlled to be 105-115 ℃, the operating pressure is controlled to be 0.08-0.14 MPaG, the temperature of the bottom of the solvent separation device is controlled to be 192-202 ℃, and the operating pressure is controlled to be 0.11-0.17 MPaG. Part of the solvent (containing byproduct methylcyclopentane) extracted from the tower top of the solvent separation device is mixed with the fresh solvent and then flows back to the solvent feeding pipeline for reuse, and part of the solvent enters the byproduct separation device.
(8) The temperature of the top of the byproduct separation device is controlled to be 70-78 ℃, the operating pressure is controlled to be 0.05-0.1 MPaG, the temperature of the bottom of the byproduct separation device is controlled to be 80-90 ℃, and the operating pressure is controlled to be 0.1-0.15 MPaG. The byproduct methylcyclopentane is extracted from the top of the byproduct separation device, the high-purity solvent (one or the combination of at least two of cyclohexane, methylcyclopentane or methylcyclohexane) is extracted from the bottom of the byproduct separation device, and the high-purity solvent flows back to the solvent feeding pipeline for reuse.
(9) The bottom discharge of the solvent separation device enters a 1-octene separation device, the temperature of the top of the 1-octene separation device is controlled at 80-85 ℃, and the operating pressure is controlled at-0.075 MPaG-0.070 MPaG. The temperature of the bottom of the 1-octene separation device is controlled to be 145-150 ℃, and the operation pressure is controlled to be-0.065 MPaG-0.060 MPaG. 1-octene products extracted from the top of the 1-octene separation device are led into the 1-octene collection device, and C is extracted from the bottom of the 1-octene separation device10 +And (4) components.
The system refers to an equipment system, or a production equipment.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) the utility model discloses an ethylene oligomerization synthesis 1-octene and 1-hexene realizes synthesizing 1-octene, 1-hexene's complete set flow through raw materials compression unit, reaction polymerization unit, termination reaction unit and product separation unit. The complete equipment realizes the production of two different products of 1-octene and 1-hexene in different working sections under the same flow, efficiently separates the reaction products according to the sequence of the boiling points of the reaction products from low to high, greatly saves the equipment investment, reduces the production energy consumption, and can adjust the proportion of the two products according to the production requirements.
(2) The heat of polymerization reaction in the reaction device is timely removed, so that the equilibrium and stability of the reaction temperature are ensured, and the wall sticking phenomenon of polymerization byproducts in subsequent equipment and pipelines is favorably reduced.
(3) The reaction is quickly terminated in time through the innovative design of the termination reaction device, and the generation of polymerization byproducts is reduced, so that the influence of the polymerization byproducts on the wall sticking of subsequent equipment and pipelines is greatly reduced.
Drawings
Fig. 1 is a schematic structural diagram of a production system according to an embodiment of the present invention.
Wherein, 1-a compression device; 2-a reaction device; 3-a circulating pump; 4-a cooling device; 5-terminating the reaction apparatus; 6-a flash evaporation device; 7-a deethylenizer; an 8-1-hexene separation unit; 9-a solvent separation unit; a 10-1-octene separation unit; 11-byproduct separation unit.
Detailed Description
In the description of the present invention, it should be noted that unless otherwise explicitly stated or limited, the terms "disposed," "connected," and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
In a specific embodiment, the utility model provides a production system for 1-octene and 1-hexene are synthesized in the oligomerization of ethylene, the production system as shown in figure 1, including raw materials compression unit, reaction polymerization unit, termination reaction unit and product separation unit that connect gradually.
The feed compression unit comprises a compression device 1, said compression device 1 being adapted to compress an ethylene feed.
The reaction polymerization unit comprises a reaction device 2, and a catalyst injection port and a cocatalyst injection port are arranged at the upper part, the middle part and the lower part of the reaction device 2. In this embodiment, the reaction apparatus 2 may optionally employ a stirred tank reactor. A solvent feeding pipeline is externally connected to a connecting pipeline between the compression device 1 and the reaction device 2, and the ethylene raw material is compressed by the compression device 1 and then mixed with the solvent introduced into the solvent feeding pipeline to enter the reaction device 2. The inner coil is arranged in the reaction device 2, the adopted inner coil is of a spiral structure, and the interior of the reaction device 2 is cooled by introducing a cooling medium into the inner coil. The outer side of the shell of the reaction device 2 is provided with a jacket, and a cooling medium is introduced into the jacket to cool the interior of the reaction device 2. The reaction polymerization unit further comprises a circulating heat removal device, the circulating heat removal device comprises a circulating pipeline, one end of the circulating pipeline is connected into a bottom circulating outlet of the reaction device 2, the other end of the circulating pipeline is connected into a top circulating inlet of the reaction device 2, the circulating pipeline is sequentially provided with a circulating pump 3 and a cooling device 4 along the flow direction of reaction liquid.
The termination reaction unit comprises a termination reaction device 5, the upper part and the middle part of the termination reaction device 5 are both provided with a terminator inlet, and the ethylene oligomerization synthesis reaction is terminated by injecting a terminator into the termination reaction device 5. The upper overflow port of the reaction device 2 is connected with the liquid inlet of the termination reaction device 5 through an overflow pipe, the reaction product flows through the overflow pipe from the overflow port and enters the termination reaction device 5, the overflow pipe is obliquely and downwards arranged along the flow direction of the reaction product, and the included angle between the overflow pipe and the horizontal direction is any one angle of 20-45 degrees. In this embodiment, the termination reaction device 5 may optionally employ a stirred tank reactor.
An ethylene removal unit is also arranged between the reaction termination unit and the product separation unit and is used for removing unreacted ethylene raw materials in reaction products. The ethylene removal unit comprises a flash evaporation device 6 and a deethylenizer 7 which are sequentially connected, a liquid outlet at the bottom of the termination reaction device 5 is connected with a liquid inlet of the flash evaporation device 6, an outlet at the top of the flash evaporation device 6 is externally connected with an ethylene gas collecting device, and a liquid outlet at the bottom of the flash evaporation device 6 is connected with a liquid inlet of the deethylenizer 7. The top collecting port of the ethylene removing device 7 is externally connected with an ethylene gas collecting device, and the bottom liquid outlet of the ethylene removing device 7 is connected with the liquid inlet of the 1-hexene separating device 8.
The product separation unit comprises a 1-hexene separation device 8, a solvent separation device 9, a 1-octene separation device 10 and a byproduct separation device 11 which are connected in sequence, and the specific connection relationship among the four devices is as follows:
the top outlet of the 1-hexene separating device 8 is connected with a 1-hexene collecting device, 1-hexene is collected from the top of the 1-hexene separating device 8 and enters the 1-hexene collecting device, and the bottom liquid outlet of the 1-hexene separating device 8 is connected with the liquid inlet of the solvent separating device 9.
The tower top outlet of the solvent separation device 9 is divided into two paths, one path is connected to a solvent feeding pipeline, the other path is connected to a liquid inlet of the byproduct separation device 11, and a liquid outlet at the bottom of the solvent separation device 9 is connected to a liquid inlet of the 1-octene separation device 10.
A liquid outlet at the bottom of the byproduct separating device 11 is connected with a solvent feeding pipeline, the solvent obtained by separation is extracted from the bottom of the tower and flows back to the solvent feeding pipeline, the byproduct obtained by separation of the byproduct separating device 11 is discharged from the top of the tower, and the byproduct comprises methylcyclopentane.
The outlet of the 1-octene separating device 10 is connected with a 1-octene collecting device, and 1-octene is extracted from the top of the 1-octene separating device 10 and then enters the 1-octene collecting device.
The applicant states that the above description is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and those skilled in the art should understand that any changes or substitutions easily conceivable by those skilled in the art within the technical scope of the present invention are within the protection scope and the disclosure scope of the present invention.
Claims (10)
1. A production system for synthesizing 1-octene and 1-hexene by ethylene oligomerization is characterized by comprising a raw material compression unit, a reaction polymerization unit, a reaction termination unit and a product separation unit which are sequentially connected;
the product separation unit comprises a 1-hexene separation device and a 1-octene separation device which are sequentially connected.
2. The production system according to claim 1, wherein the feed compression unit comprises a compression device for compressing an ethylene feed.
3. The production system of claim 2, wherein the reactive polymerization unit comprises a reaction device;
the upper part, the middle part and the lower part of the reaction device are provided with a catalyst injection port and a cocatalyst injection port;
the reaction device is a stirred tank reactor.
4. The production system of claim 3, wherein a solvent feed line is externally connected to the connection line between the compression device and the reaction device, and the ethylene raw material is compressed by the compression device and then mixed with the solvent introduced into the solvent feed line to enter the reaction device.
5. The production system of claim 4, wherein an inner coil is arranged in the reaction device, the inner coil is of a spiral structure, and a cooling medium is introduced into the inner coil to cool the interior of the reaction device.
6. The production system of claim 5, wherein a jacket is arranged outside the shell of the reaction device, and a cooling medium is introduced into the jacket to cool the interior of the reaction device.
7. The production system of claim 6, wherein the reaction polymerization unit further comprises a circulation heat removal device, the circulation heat removal device comprises a circulation pipeline, one end of the circulation pipeline is connected to a bottom circulation outlet of the reaction device, the other end of the circulation pipeline is connected to a top circulation inlet of the reaction device, and a circulation pump and a cooling device are sequentially arranged on the circulation pipeline along the flow direction of the reaction solution.
8. The production system of claim 7, wherein the termination reaction unit comprises a termination reaction device, and the termination reaction device is filled with a terminator to terminate the ethylene oligomerization synthesis reaction;
the reaction terminating device is a stirred tank reactor;
the length-diameter ratio of the reaction terminating device is 3.0-6.0;
the upper part and the middle part of the reaction terminating device are both provided with a terminating agent inlet;
the upper overflow port of the reaction device is connected with the liquid inlet of the reaction termination device through an overflow pipe, and a reaction product flows through the overflow pipe from the overflow port and enters the reaction termination device;
the overflow pipe is obliquely arranged downwards along the flow direction of the reaction products;
the included angle between the overflow pipe and the horizontal direction is 20-45 degrees.
9. The production system according to claim 8, wherein an ethylene removal unit is further arranged between the reaction terminating unit and the product separation unit, and the ethylene removal unit is used for removing unreacted ethylene raw materials in the reaction product;
the ethylene removal unit comprises a flash evaporation device and a deethylenizer which are sequentially connected;
a liquid outlet at the bottom of the reaction terminating device is connected with a liquid inlet of the flash evaporation device, a liquid outlet at the top of the flash evaporation device is externally connected with an ethylene gas collecting device, and a liquid outlet at the bottom of the flash evaporation device is connected with a liquid inlet of the ethylene removing device;
the top collecting port of the ethylene removing device is externally connected with an ethylene gas collecting device, and the bottom liquid outlet of the ethylene removing device is connected with the liquid inlet of the 1-hexene separating device.
10. The production system according to claim 9, wherein the product separation unit further comprises a solvent separation device and a byproduct separation device, the solvent separation device being disposed between the 1-hexene separation device and the 1-octene separation device along the product separation route;
a top outlet of the 1-hexene separation device is connected with a 1-hexene collection device, and 1-hexene is collected from the top of the 1-hexene separation device and then enters the 1-hexene collection device; a liquid outlet at the bottom of the 1-hexene separation device is connected with a liquid inlet of the solvent separation device;
the top extraction port of the solvent separation device is divided into two paths, one path is connected to a solvent feeding pipeline, and the other path is connected with the liquid inlet of the byproduct separation device; a liquid outlet at the bottom of the solvent separation device is connected with a liquid inlet of the 1-octene separation device;
a liquid outlet at the bottom of the byproduct separation device is connected with a solvent feeding pipeline, a solvent obtained by separation is extracted from the bottom of the tower and flows back to the solvent feeding pipeline, a byproduct obtained by separation of the byproduct separation device is discharged from the top of the tower, and the byproduct comprises methylcyclopentane;
and a production outlet at the top of the 1-octene separation device is connected with a 1-octene collection device, and 1-octene enters the 1-octene collection device after being produced from the top of the 1-octene separation device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921865342.4U CN210855896U (en) | 2019-10-31 | 2019-10-31 | Production system for synthesizing 1-octene and 1-hexene through ethylene oligomerization |
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| CN201921865342.4U CN210855896U (en) | 2019-10-31 | 2019-10-31 | Production system for synthesizing 1-octene and 1-hexene through ethylene oligomerization |
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