WO2021033971A1 - Procédé de préparation d'oligomère et dispositif de préparation d'oligomère - Google Patents

Procédé de préparation d'oligomère et dispositif de préparation d'oligomère Download PDF

Info

Publication number
WO2021033971A1
WO2021033971A1 PCT/KR2020/010466 KR2020010466W WO2021033971A1 WO 2021033971 A1 WO2021033971 A1 WO 2021033971A1 KR 2020010466 W KR2020010466 W KR 2020010466W WO 2021033971 A1 WO2021033971 A1 WO 2021033971A1
Authority
WO
WIPO (PCT)
Prior art keywords
separation device
stream
discharge stream
reactor
monomer
Prior art date
Application number
PCT/KR2020/010466
Other languages
English (en)
Korean (ko)
Inventor
김은교
김미경
신준호
김혜빈
Original Assignee
주식회사 엘지화학
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from KR1020200094665A external-priority patent/KR102602865B1/ko
Application filed by 주식회사 엘지화학 filed Critical 주식회사 엘지화학
Priority to US17/424,426 priority Critical patent/US11384035B2/en
Priority to JP2021541111A priority patent/JP7195688B2/ja
Priority to EP20855444.4A priority patent/EP3892607A4/fr
Publication of WO2021033971A1 publication Critical patent/WO2021033971A1/fr

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series

Definitions

  • the present invention relates to an oligomer manufacturing method and an oligomer manufacturing apparatus, and more particularly, to an oligomer manufacturing method and an oligomer manufacturing apparatus for efficiently recycling the monomers recovered in the oligomer manufacturing process.
  • Alpha-olefin is an important material used in comonomers, detergents, lubricants, plasticizers, etc., and is widely used commercially.
  • 1-hexene and 1-octene control the density of polyethylene in the production of linear low-density polyethylene (LLDPE). It is widely used as a comonomer for regulation.
  • LLDPE linear low-density polyethylene
  • Alpha olefins such as 1-hexene and 1-octene are typically produced through an oligomerization reaction of ethylene.
  • the ethylene oligomerization reaction is carried out by an oligomerization reaction (trimerization reaction or tetramerization reaction) of ethylene using ethylene as a reactant, and the product produced through the reaction contains the desired 1-hexene and 1-octene. It contains unreacted ethylene as well as multi-component hydrocarbon mixtures.
  • the product is subjected to a separation process through a distillation column, and at this time, unreacted ethylene is recovered and reused for the ethylene oligomerization reaction.
  • a separation device such as a distillation column or a flash drum is used to reduce the amount of products or by-products such as solvents in the recovered unreacted ethylene stream.
  • the difference in boiling point between the unreacted ethylene and the product is large, so that the difference in upper and lower temperatures of the separation device is also large.
  • the upper and lower temperatures of the separating device are determined according to the pressure of the separating device. When the pressure of the separating device is high, the upper and lower temperatures are increased, and when the pressure of the separating device is low, the upper and lower temperatures are lowered.
  • the conventional method for recovering unreacted ethylene and reusing it for the oligomerization reaction has high investment costs, such as lowering the production yield of the product, using a refrigerant having a very low temperature, or installing a compressor having a high compression ratio, There is a problem with poor economics.
  • the problem to be solved in the present invention is to provide an oligomer manufacturing method and an oligomer manufacturing apparatus with reduced investment cost in order to solve the problems mentioned in the technology behind the present invention.
  • the present invention comprises the steps of performing an oligomerization reaction by supplying a feed stream containing a monomer to a reactor; Supplying a first discharge stream of the reactor to a first separation device, and supplying a second discharge stream of the reactor to a second separation device; Recovering the monomer to the upper discharge stream of the second separation device, and feeding the lower discharge stream to a third separation device; And supplying the upper discharge stream of the third separation device to a second separation device.
  • the present invention is a reactor for oligomerizing a feed stream containing the supplied monomer, supplying a first discharge stream to a first separation device, and supplying a second discharge stream to a second separation device;
  • a first separation device receiving the reactor first discharge stream;
  • a second separation device for receiving the second discharge stream of the reactor, recovering the monomer as an upper discharge stream, and supplying the lower discharge stream to a third separation device;
  • a third separation device configured to receive the second separation device lower discharge stream and supply the upper discharge stream to the second separation device.
  • the second separation device in recovering the unreacted monomer, is operated at high pressure, and the third separation device to which the lower discharge stream of the second separation device is connected is operated at low pressure.
  • the lower stream of the second separation device has a boiling point higher than a monomer and a boiling point lower than an oligomer product.
  • the by-product can be concentrated. Accordingly, by operating the second separation device at high pressure, the upper temperature is maintained at a high temperature and the lower temperature is lowered, thereby efficiently recovering the monomer and suppressing side reactions of hydrocarbons.
  • FIG. 1 is a process flow diagram according to a method for manufacturing an oligomer according to an embodiment of the present invention.
  • the term'stream' may mean a flow of a fluid in a process, and may also mean a fluid itself flowing in a pipe. Specifically, the'stream' may mean the fluid itself and the flow of the fluid simultaneously flowing in a pipe connecting each device. In addition, the fluid may mean gas or liquid.
  • a method for preparing an oligomer is provided.
  • the step of performing an oligomerization reaction by supplying a feed stream containing a monomer to a reactor; Supplying a first discharge stream of the reactor to a first separation device, and supplying a second discharge stream of the reactor to a second separation device; Recovering the monomer to the upper discharge stream of the second separation device, and feeding the lower discharge stream to a third separation device; And supplying the top discharge stream of the third separation device to a second separation device.
  • a feed stream containing a monomer is supplied to the reactor, and the monomer is in a liquid phase at the bottom of the reactor.
  • the oligomerization reaction of can be carried out.
  • the oligomerization reaction may mean a reaction in which a monomer is micropolymerized. Depending on the number of monomers to be polymerized, they are called trimerization and tetramerization, and these are collectively referred to as multimerization.
  • the monomer may be ethylene
  • the oligomer may be an alpha olefin.
  • Alpha olefin is an important material used for comonomers, detergents, lubricants, plasticizers, etc., and is widely used commercially.
  • 1-hexene and 1-octene are balls for controlling the density of polyethylene in the manufacture of linear low-density polyethylene (LLDPE). It is widely used as a monomer.
  • Alpha olefins such as 1-hexene and 1-octene may be prepared, for example, through a trimerization reaction or tetramerization reaction of ethylene.
  • the step of the oligomerization reaction of the monomer may be carried out in a reactor suitable for a continuous process, preferably selected from the group consisting of a continuous stirred reactor (CSTR) and a plug flow reactor (PFR). It can be carried out under a reaction system comprising one or more reactors.
  • a reactor suitable for a continuous process preferably selected from the group consisting of a continuous stirred reactor (CSTR) and a plug flow reactor (PFR). It can be carried out under a reaction system comprising one or more reactors.
  • the oligomerization reaction of the monomer is a homogeneous liquid phase reaction in the presence or absence of a solvent by applying a conventional contact technique with the reaction system, a form in which some or all of the catalyst system is not dissolved. It can be carried out as a phosphorus slurry reaction, a two-phase liquid/liquid reaction, or as a bulk or gaseous reaction in which the product acts as the main medium.
  • the step of the oligomerization reaction of the monomer may be performed as a homogeneous liquid phase reaction.
  • the step of performing the oligomerization reaction may be performed at a temperature of 10°C to 180°C, 30°C to 150°C, or 50°C to 120°C .
  • the step of performing the oligomerization reaction may be performed under a pressure of 15 bar to 100 bar, 20 bar to 80 bar, or 25 bar to 60 bar.
  • the feed stream including the monomer may include a vapor phase monomer and a solvent.
  • the gaseous monomer contained in the feed stream may be supplied as a feed stream containing the monomer directly or after a storage step of the ethylene monomer separated in a Naphtha Cracking Center (NCC) process.
  • the gaseous monomer may include a stream recovered in the oligomer manufacturing process.
  • the solvent contained in the feed stream may be supplied to the reactor as a feed stream.
  • the solvent recovered after use in the oligomer process may be reused.
  • the separation device in the step of supplying the first discharge stream of the reactor to the first separation device and supplying the second discharge stream of the reactor to the second separation device, the separation device comprises a conventional distillation column. Can be used.
  • the first discharge stream may be a stream containing a gaseous monomer.
  • an upper discharge stream including gaseous monomers may be supplied to a reactor, and a lower discharge stream including liquid monomers may be supplied to a second separation device.
  • the upper discharge stream of the first separation device may be mixed with a gaseous monomer stream separately supplied to the reactor and supplied to the reactor by mixing in a mixer, or may be separately supplied to the reactor.
  • the reactor second discharge stream may be supplied to a second separation device to be separated into an upper discharge stream containing a gaseous monomer and a lower discharge stream containing an oligomer product, a byproduct, and a solvent.
  • the gaseous monomer recovered as an upper discharge stream in the second separation device may be supplied to the reactor.
  • the second separation device upper discharge stream may be mixed with the gaseous monomer stream and the first separation device upper discharge stream separately supplied to the reactor and supplied to the reactor by mixing in a mixer, or may be separately supplied to the reactor.
  • the second separation unit bottom effluent stream is fed to a third separation unit to be separated in a third separation unit into a liquid bottom effluent stream containing oligomers and solvents and a liquid top effluent stream containing C4 compounds as by-products.
  • the C4 compound may include 1-butene (1-C4).
  • the content of the C4 compound contained in the upper discharge stream of the third separation device may be 70% by weight or more.
  • the content of the C4 compound contained in the upper discharge stream of the third separation device may range from 70% to 99% by weight, 80% to 95% by weight, or 85% to 90% by weight.
  • the upper discharge stream of the third separation device including the C4 compound may be supplied to the second separation device, while the second separation device and the third separation device may have a circulation flow.
  • the C4 compound having a lower boiling point compared to the oligomer product and the solvent may be concentrated in the lower portion of the second separation device.
  • the content of the concentrated C4 compound in the lower discharge stream of the second separation device may be 5% to 40% by weight.
  • the content of the C4 compound contained in the lower discharge stream of the second separation device may be 5% to 40% by weight, 10% to 30% by weight, or 13% to 20% by weight.
  • the second separation unit lower discharge stream containing the concentrated C4 compound is fed to a third separation unit, and the upper discharge stream containing 80% by weight or more C4 compounds is discharged from the third separation unit.
  • the C4 compound can be efficiently separated by a method of branching and recovering some streams of the upper discharge stream of the third separation device to the second separation device.
  • the C4 compound may be selectively recovered by partially purging the upper discharge stream of the third separation device containing the C4 compound in a high content.
  • the content of the C4 compound contained in some streams of the upper discharge stream of the third separation device may be 70% by weight or more.
  • the content of the C4 compound contained in some streams of the upper discharge stream of the third separation device may range from 70% to 99% by weight, 80% to 95% by weight, or 85% to 90% by weight.
  • the content of monomers in some streams of the upper discharge stream of the third separation device may be 5% by weight or less.
  • the content of the monomer contained in some streams of the upper discharge stream of the third separation device may range from 0.01% to 5% by weight, from 0.1% to 3% by weight, or from 0.5% to 2% by weight.
  • the oligomer manufacturing method according to the present invention minimizes the loss of monomer to 5% by weight or less, while purging some streams of the upper discharge stream of the third separation device to selectively recover the C4 compound as a by-product in the process. I can.
  • the C4 compound is removed by purging some streams of the unreacted monomer recovery stream without a separate C4 separation step due to low selectivity for the C4 compound in the conventional oligomer production method, the monomer is also removed along with the C4 compound, The problem that the loss of monomer was large was solved.
  • the content ratio of the C4 compound contained in the upper discharge stream of the third separation device to the content of the C4 compound contained in the second discharge stream of the reactor may be 2 or more and 2 to 7, 4 to 6.
  • the upper discharge stream of the third separation device may mean a stream discharged from the upper portion of the third separation device and supplied to the second separation device.
  • the content ratio of the C4 compound contained in the upper discharge stream of the third separation device to the content of the C4 compound contained in the second discharge stream of the reactor is determined by supplying the second discharge stream of the reactor to the second separation device, and the third It may mean a concentration ratio at which the C4 compound is concentrated in the second discharge stream of the reactor while partially circulating through the separation device.
  • the second separation device by installing a third separation device at the rear end of the second separation device to concentrate the C4 compound at a concentration ratio of at least twice the C4 content in the second discharge stream of the reactor, the second separation device because the boiling point of the C4 compound is low. It is possible to obtain the effect of lowering the boiling point of the lower discharge stream of, and thus lower the temperature of the lower part while maintaining the pressure of the second separation device at high pressure. Specifically, when the concentration of the substance having a low boiling point is increased at the same pressure, the boiling point of the mixture is lowered, and thus the boiling point of the lower discharge stream of the second separation device can be lowered by concentrating the C4 compound.
  • the boiling point of the stream discharged from the distillation column may refer to an operating temperature of the corresponding distillation column
  • the boiling point of the lower discharge stream of the second separation device may refer to an operation temperature under the second separation unit.
  • the pressure in the second separation device may be operated at a higher pressure than the pressure in the third separation device.
  • the second separation device may lower the bottom temperature while maintaining the upper temperature of the second separation device at a high temperature by discharging the lower discharge stream containing the monomer to the third separation device while operating at high pressure.
  • side reactions of hydrocarbons can be suppressed.
  • by operating the pressure in the second separation device at high pressure while maintaining the upper temperature at a high temperature and lowering the lower temperature unreacted monomers can be easily recovered from the upper part, and the oligomer produced at the lower part is decomposed, or other substances It is possible to prevent the occurrence of side reactions that react with and generate by-products.
  • the pressure in the second separation device may range from 12 bar to 25 bar, and the pressure in the third separation device may range from 3 bar to 15 bar.
  • the pressure in the second separation device may be 12 bar to 25 bar, 13 bar to 23 bar, or 14 bar to 20 bar
  • the pressure in the third separation device is 3 bar to 15 bar, 4 bar to 13 bar. bar or 5 bar to 10 bar range.
  • the second separation device is operated at a high pressure, and the lower discharge stream of the second separation device is supplied to a third separation device operated at a low pressure, and a circulation flow between the high pressure second separation device and the low pressure third separation device
  • the temperature of the lower discharge stream of the second separation device may be 130 °C to 200 °C.
  • the temperature of the lower discharge stream of the second separation device may be 130°C to 200°C, 140°C to 190°C, or 150°C to 180°C.
  • the solvent and the oligomer may be separated through an additional separation process, and the separated solvent may be supplied to the reactor.
  • the separated oligomer may be separated into monomer trimers and tetramers through an additional separation process.
  • an apparatus for producing an oligomer comprising: a reactor for oligomerizing a feed stream containing a supplied monomer, supplying a first discharge stream to a first separation device, and supplying a second discharge stream to a second separation device; A first separation device receiving the reactor first discharge stream; A second separation device for receiving the second discharge stream of the reactor, recovering the monomer as an upper discharge stream, and supplying the lower discharge stream to a third separation device; And a third separation device configured to receive the second separation device lower discharge stream and supply the upper discharge stream to the second separation device.
  • the apparatus for manufacturing an oligomer according to the present invention may be an apparatus for performing a process according to the method for manufacturing an oligomer described above.
  • the apparatus for producing an oligomer according to the present invention may be described with reference to FIG. 1 below.
  • the oligomer production apparatus includes a reactor 100 for oligomerizing a feed stream containing supplied monomers, and in the reactor 100, a first discharge stream containing a gaseous monomer is first
  • the second discharge stream is supplied to the separation device 200 and includes a liquid monomer may be supplied to the second separation device 210.
  • the feed stream supplied to the reactor 100 may include a monomer and a solvent.
  • the feed stream may contain a gaseous monomer and a solvent.
  • the feed stream containing the gaseous monomer is a gaseous monomer stream directly supplied to the reactor 100, a gaseous monomer recovered as an upper discharge stream from the first separation device 200, and a second separation device 210 It may contain a gaseous monomer recovered as an upper discharge stream at.
  • the gaseous monomer stream directly supplied to the reactor 100, the upper discharge stream of the first separation device 200 including the gaseous monomer, and the second separation device 210 upper discharge stream including the gaseous monomer are individually It may be supplied to the reactor 100 or may be supplied to the reactor 100 as a mixed discharge stream mixed in a mixer (not shown).
  • the solvent may be separately supplied to the reactor 100, and in this case, the solvent separated after use in the process may be reused.
  • the first separation device 200 receives the first discharge stream from the reactor 100 and converts the upper discharge stream including the gaseous monomer into the lower discharge stream including the liquid monomer. Can be separated.
  • the upper discharge stream of the first separation device 200 may be supplied to the reactor 100, and the lower discharge stream may be supplied to the second separation device 210.
  • the second separation device 210 receives the second discharge stream of the reactor 100 including the liquid monomer and the lower discharge stream of the first separation device 200, It can be separated into a top effluent stream comprising monomers and a bottom effluent stream comprising oligomeric products, by-products and solvents.
  • the upper discharge stream of the second separation device 210 may be supplied to the reactor 100, and the lower discharge stream may be supplied to the third separation device 220.
  • the upper discharge stream of the second separation device 210 may pass through the compressor 300 and be supplied to the reactor 100.
  • the second separation device 210 since the second separation device 210 is operated at a high pressure of 12 bar to 20 bar, there is an advantage of being economical in that a compressor 300 having a relatively low compression ratio may be used. Therefore, compared to the case of using the conventional high compression ratio compressor 300, it is possible to reduce the process cost.
  • the lower discharge stream of the second separation device 210 may be supplied to the third separation device 220, and an upper discharge stream including a by-product including a C4 compound may be supplied to the second separation device 210.
  • the upper discharge stream of the third separation device 220 may be supplied to the second separation device 210 using the pump 400.
  • the pump 400 is used to supply the upper discharge stream of the third separation device 220 to the second separation device 210, in which the pressure of the upper discharge stream of the third separation device 220 is The pressure of the second separation device 210 may be increased.
  • Some streams of the upper discharge stream of the third separation device 220 may be recovered without being supplied to the second separation device 210. Specifically, the upper discharge stream of the third separation device 220 may be purged to recover some of the streams including the C4 compound, and the remaining stream may be supplied to the second separation device 210.
  • a bottom effluent stream including an oligomer product and a solvent may be recovered.
  • the oligomer product and the solvent contained in the lower discharge stream of the third separation device 220 may be separated through an additional separation device (not shown), and the separated solvent may be reused in the oligomer manufacturing process.
  • the oligomer product may include 1-hexene and 1-octene.
  • the 1-hexene and 1-octene may be separated through an additional separation device (not shown) or may be separated and used through a separate process.
  • a condenser (not shown) is provided above at least one of the first separation device 200, the second separation device 210, and the third separation device 220. May be additionally installed, and a reboilier (not shown) may be additionally installed in the lower part.
  • the process was simulated using an Aspen Plus simulator manufactured by Aspen Tech.
  • the lower discharge stream of the second separation device 210 is a stream that has passed through a reboiler (not shown), and the upper discharge stream of the third separation device 220 passes through a condenser (not shown). It is one stream, and the lower discharge stream of the third separation device 220 is a stream that has passed through a reboiler (not shown).
  • ethylene (C2) as a monomer was supplied to the reactor 100 at a reaction amount of 20,000 kg/hr or more, and the reaction conditions of the reactor 100 were set at a temperature of 53° C. and a pressure of 30 bar, and the second separation The operating pressure of the device 210 was set to 15 bar, and the operating pressure of the third separation device 220 was set to 6 bar.
  • Table 1 The results are shown in Table 1 below.
  • the component flow rate in the stream is described by rounding to the first decimal place, and when the flow rate is expressed in weight%, it is calculated and described as the component flow rate content in the total flow rate.
  • the second separation device 210 and the third separation device 220 compared to the content of 1-C4 in the second discharge stream of the reactor 100 supplied to the second separation device 210 It can be seen that the content ratio of 1-C4 in the stream circulated back to the second separation device 210, that is, the concentration ratio of 1-C4, is concentrated to about 4.6, and as a result, the lower discharge stream of the second separation device 210 It could be seen that the content of 1-C4 in it was 17% by weight.
  • the content of 1-C4 in the separated stream by purging a partial stream of the upper discharge stream of the third separation device 220 is 85% by weight
  • the content of ethylene monomer is 1% by weight
  • the purity of 1-C4 is It is high, and it can be seen that there is little loss of ethylene monomer.
  • the operation pressure of the second separation device 210 was set to 18 bar, and the operation pressure of the third separation device 220 was set to 8 bar .
  • the results are shown in Table 2 below.
  • the operating pressure of the second separation device 210 when the operating pressure of the second separation device 210 is set to 18 bar, and the operating pressure of the third separation device 220 is set to 8 bar, the upper portion of the third separation device 220 In the separated stream by purging some streams of the discharge stream, the content of 1-C4 is 80% by weight, the content of ethylene monomer is 2% by weight, the purity of 1-C4 is high, and the loss of ethylene monomer is almost
  • the pressure of the second separation device 210 is high, but the concentration flow and the concentration ratio of 1-C4 are increased by increasing the fifth stream, so that the second separation device ( 210)
  • the temperature of the lower discharge stream could be operated at 160 °C in the same manner as in Example 1.
  • the process was simulated using the Aspen Plus simulator of Aspen Tech.
  • the upper discharge stream of the second separation device 210 is a stream that has passed through a condenser (not shown), and the lower discharge stream of the second separation device 210 passes through a reboiler (not shown). It's a stream.
  • ethylene (C2) as a monomer was supplied to the reactor 100 at a reaction amount of 20,000 kg/hr or more, and the reaction conditions of the reactor 100 were set at a temperature of 53° C. and a pressure of 30 bar, and the second separation The operating pressure of the device 210 was set to 15 bar.
  • Table 3 The results are shown in Table 3 below.
  • the second separation device 210 is operated at 15 bar as in Example 1, but if you look at the 3-1 stream, which is the lower discharge stream of the second separation device 210, , It can be seen that the temperature is 212 °C, which is significantly higher compared to the 160 °C of Example 1. In addition, even in the case of Example 2 where the operating pressure of the second separation device 210 is higher than 15 bar, the temperature of the lower discharge stream of the second separation device 210 is 160° C., which is significantly higher than that of Comparative Example 1.
  • the separation device 210 In addition, in the case of Examples 1 and 2, compared with the 1-C4 content in the lower discharge stream of the second separation device 210 is 17% by weight and 19% by weight, in the case of the comparative example, the separation device 210 It can be seen that the 1-C4 content in the bottom effluent stream is less than 0.5% by weight.
  • Comparative Example 2 the comparative example above except that the operating pressure of the second separation device 210 was set to 6 bar in order to lower the lower temperature of the second separation device 210 to 160 °C as in Example 1. It was carried out in the same manner as in 2. The results are shown in Table 4 below.
  • the temperature of the stream 3-1 which is the lower discharge stream of the second separation device 210, is 160 as in Example 1.
  • the compression ratio is generally 3 times higher. It was confirmed that two compressors 300 should be used as shown in FIG. 3 below.
  • the temperature of the 3-1 stream was lowered. The temperature of the 2-1 stream was also lowered to -16°C.
  • a refrigerant having a lower temperature level than refrigerants such as cooling water and ethylene glycol antifreeze generally used in the process must be used. There is a problem that driving costs are incurred.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention se rapporte à un procédé de préparation d'oligomère et concerne un procédé et un dispositif de préparation d'oligomère, le procédé de préparation d'oligomère comprenant les étapes consistant à : mettre en œuvre une réaction d'oligomérisation par alimentation d'un réacteur avec un flux d'alimentation contenant un monomère ; fournir un premier flux de décharge du réacteur à un premier séparateur, et fournir un second flux de décharge du réacteur à un deuxième séparateur ; récupérer le monomère par un flux de décharge supérieur du deuxième séparateur, et fournir un flux de décharge inférieur de celui-ci à un troisième séparateur ; et fournir un flux de décharge supérieur du troisième séparateur au deuxième séparateur.
PCT/KR2020/010466 2019-08-21 2020-08-07 Procédé de préparation d'oligomère et dispositif de préparation d'oligomère WO2021033971A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US17/424,426 US11384035B2 (en) 2019-08-21 2020-08-07 Oligomer preparation method and oligomer preparation device
JP2021541111A JP7195688B2 (ja) 2019-08-21 2020-08-07 オリゴマーの製造方法およびオリゴマーの製造装置
EP20855444.4A EP3892607A4 (fr) 2019-08-21 2020-08-07 Procédé de préparation d'oligomère et dispositif de préparation d'oligomère

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
KR20190102511 2019-08-21
KR10-2019-0102511 2019-08-21
KR1020200094665A KR102602865B1 (ko) 2019-08-21 2020-07-29 올리고머 제조 방법 및 올리고머 제조 장치
KR10-2020-0094665 2020-07-29

Publications (1)

Publication Number Publication Date
WO2021033971A1 true WO2021033971A1 (fr) 2021-02-25

Family

ID=74660537

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2020/010466 WO2021033971A1 (fr) 2019-08-21 2020-08-07 Procédé de préparation d'oligomère et dispositif de préparation d'oligomère

Country Status (1)

Country Link
WO (1) WO2021033971A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070185362A1 (en) * 2006-02-03 2007-08-09 Lattner James R Process for generating alpha olefin comonomers
WO2012039838A2 (fr) * 2010-09-21 2012-03-29 Synfuels International, Inc. Système et procédé pour la production de combustibles liquides
US20130102826A1 (en) * 2011-05-24 2013-04-25 James R. Lattner Systems And Methods For Generating Alpha Olefin Oligomers
US20130296483A1 (en) * 2011-01-13 2013-11-07 Idemitsu Kosan Co, Ltd. Method for producing olefin oligomer mixture
US20160368834A1 (en) * 2015-06-16 2016-12-22 Siluria Technologies, Inc. Ethylene-to-liquids systems and methods

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070185362A1 (en) * 2006-02-03 2007-08-09 Lattner James R Process for generating alpha olefin comonomers
WO2012039838A2 (fr) * 2010-09-21 2012-03-29 Synfuels International, Inc. Système et procédé pour la production de combustibles liquides
US20130296483A1 (en) * 2011-01-13 2013-11-07 Idemitsu Kosan Co, Ltd. Method for producing olefin oligomer mixture
US20130102826A1 (en) * 2011-05-24 2013-04-25 James R. Lattner Systems And Methods For Generating Alpha Olefin Oligomers
US20160368834A1 (en) * 2015-06-16 2016-12-22 Siluria Technologies, Inc. Ethylene-to-liquids systems and methods

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3892607A4 *

Similar Documents

Publication Publication Date Title
JP2015535529A (ja) エチレンのオリゴマー化プロセス
WO2017069446A1 (fr) Procédé de séparation d'un réactif d'oligomérisation de l'éthylène
EP1777208B1 (fr) Procédé d'oligomérisation d'éthylène et réacteur à cet effet avec dispositif de refroidissement
WO2012115422A2 (fr) Procédé pour préparer un composé d'éther mono-tert-butylique de glycol
EP1713839B1 (fr) Procede de preparation de polyolefines en suspension
WO2021033993A1 (fr) Procédé de préparation d'oligomères et appareil de préparation d'oligomères
WO2021033971A1 (fr) Procédé de préparation d'oligomère et dispositif de préparation d'oligomère
WO2015190801A1 (fr) Procédé de préparation de butadiène par réaction de déshydrogénation oxydative
KR20210023692A (ko) 올리고머 제조 방법 및 올리고머 제조 장치
WO2021033972A1 (fr) Procédé de production d'oligomères et appareil de production d'oligomères
KR102592638B1 (ko) 알파 올레핀 제조 방법 및 알파 올레핀 제조 장치
US20200407300A1 (en) Method and apparatus for decomposing phenolic by-product
WO2021033957A1 (fr) Procédé de préparation et dispositif de préparation d'une alpha-oléfine
WO2021118008A1 (fr) Appareil de préparation d'oligomère
US11952339B2 (en) Method of recovering unreacted ethylene in ethylene oligomerization process
WO2019027165A2 (fr) Procédé de purification de raffinat-2
WO2022050788A1 (fr) Procédé de préparation d'oligomère
WO2022154398A1 (fr) Procédé de préparation d'oligomère
WO2021118010A1 (fr) Procédé de préparation de dimère d'acrylonitrile
WO2022097886A1 (fr) Appareil de préparation d'oligomère
WO2024038972A1 (fr) Procédé d'élimination de polymère dans un réacteur d'oligomérisation d'oléfines
WO2022030784A1 (fr) Procédé de préparation de 1-butène et de propylène
WO2022255575A1 (fr) Procédé de préparation d'alcool isopropylique
WO2022255576A1 (fr) Procédé de préparation d'alcool isopropylique
CN117529462A (zh) α-烯烃的制造方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20855444

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 20855444.4

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2021541111

Country of ref document: JP

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2020855444

Country of ref document: EP

Effective date: 20210708

NENP Non-entry into the national phase

Ref country code: DE