CN107151195A - The method that catalyst and polyethylene are removed in ethylene oligomerization production alpha-olefin technique - Google Patents
The method that catalyst and polyethylene are removed in ethylene oligomerization production alpha-olefin technique Download PDFInfo
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- CN107151195A CN107151195A CN201610118254.2A CN201610118254A CN107151195A CN 107151195 A CN107151195 A CN 107151195A CN 201610118254 A CN201610118254 A CN 201610118254A CN 107151195 A CN107151195 A CN 107151195A
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- polyethylene
- catalyst
- alkali lye
- alkali
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
- C07C2/08—Catalytic processes
- C07C2/26—Catalytic processes with hydrides or organic compounds
- C07C2/32—Catalytic processes with hydrides or organic compounds as complexes, e.g. acetyl-acetonates
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/20—Use of additives, e.g. for stabilisation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
This application discloses the method that catalyst and polyethylene are removed in a kind of ethylene oligomerization production alhpa olefin technique, comprise the following steps：S1. the reaction product for ethylene oligomerization being produced into alhpa olefin carries out flash separation, obtains liquid phase stream and the gaseous stream containing light component；S2, is passed through the alkaline cleaner containing alkali lye by liquid phase stream and carries out alkali cleaning operation, polyethylene is separated out, and is removed co-catalyst, is obtained mixture；S3, the mixture is layered, and obtains being located at undermost alkali lye layer, the intermediate layer containing polyethylene and the reaction liquid layer of the superiors.Disclosed herein as well is the device for performing methods described.The method provided according to the present invention, can effectively remove catalyst and polymer, terminate the generation of secondary response, it is ensured that product purity, prevent the operation steady in a long-term of polyethylene blocking pipeline and equipment and influence device.
Description
Technical field
The present invention relates to ethylene oligomerization field, urged with being related to remove in a kind of ethylene oligomerization production alpha-olefin technique
The method of agent and polyethylene.
Background technology
Ethylene oligomerization is one of most important reaction in olefinic polymerization industry, can will be cheap by oligomerisation reaction
Small-numerator olefin is changed into high value-added product, such as 1- hexenes and 1- octenes.Wherein, 1- hexenes are raw
LLDPE and HDPE important comonomer is produced, is also the raw material of some fine chemicals.1- hervene copolymers
LLDPE resins compared with the copolymer of 1- butylene, its tensile strength, impact strength, tear resistance and
Property durable in use is all substantially excellent, is particularly suitable for the agricultural mulch films such as packaging film and greenhouse, canopy room.But ethene is neat
Contain polymer and catalyst in polybutadiene reaction product, polymer can cause the blocking of device, the presence meeting of catalyst
Reaction solution is occurred secondary response, influence the purity of product.
The continuous production process that a kind of ethylene oligomerization prepares low-carbon alpha-alkene is reported in CN1160700A.
Using a kind of zirconium quaternary system catalyst, under specific reaction condition, by catalyst solution, ethylene raw
Gas and quencher are continuously added to corresponding course of reaction respectively, and oligomerization product draws product by continuous rectification.
Reaction actual conditions is also indicated that simultaneously, the catalyst is higher to the selectivity of carbon alkene below 10, but it is catalyzed
Activity is not high.
Ethylene oligomerization production method above all lays particular emphasis on the research of ethylene oligomerization production technology and catalyst, but
It is similar to other patents, what reaction was substantially carried out in ordinary high pressure reactor.In the prior art, it is public
A kind of method that polyethylene is removed in having opened liquid from ethylene reaction, makes polymer from reaction by way of cooling
Separate out, then filtered out from reaction solution polyethylene in liquid by filter, this method can still influence device
Continuous operation.There is a kind of method for being passed through water vapour removing polymer in the prior art, pass through steam stripping at reduced pressure
Mode reaction solution stripping is walked, polymer is stayed in aqueous phase and discharged together, and this method energy consumption is big, and
There are a large amount of discharge of wastewater.In addition, majority report is all, using conventional heat tracing technique, to maintain necessarily both at home and abroad
Temperature, makes polymer enter follow-up workshop section with reaction solution, and final and separation heavy constituent discharges dress together
Put, can thus increase energy consumption, will also result in the blocking of device.
Ethylene oligomerization technique is the polymer contained in the most frequently used production technology of worldwide production alpha-olefin, its product
And catalyst, if do not removed after the reaction, polymer can cause process pipelines to block, influence device
Continuous operation, and catalyst is not removed, and can cause the secondary response of reaction solution, influences product quality.According to
Conventional heat tracing technique, maintains certain temperature, polymer is entered follow-up workshop section with reaction solution, it is final and
The heavy constituent of separation discharger together, can thus increase energy consumption, will also result in the blocking of device.
The content of the invention
For deficiency of the prior art, the present invention is carried out using to isolating remaining reaction solution after light component
The mode of alkali cleaning, removes the generation of secondary response in co-catalyst, terminating reaction liquid, it is ensured that product purity；
Simultaneously by controlling alkali cleaning condition, especially alkali cleaning temperature, separate out ethylene oligomerization accessory substance polyethylene, so
Afterwards by layering, polymer is separated with reaction solution, polymer plugging pipeline and equipment is prevented, device is influenceed
Operation steady in a long-term；Meanwhile, also catalyst is separated from reaction solution, it is to avoid secondary response, protected
Demonstrate,prove product quality.The method according to the invention, does not interfere with the continuous operation and stable operation of device.
According to an aspect of the invention, there is provided removing catalyst in a kind of ethylene oligomerization production alpha-olefin technique
With the method for polyethylene, comprise the following steps：
S1. the reaction product for ethylene oligomerization being produced into alpha-olefin carries out flash separation, obtains liquid phase stream and containing light
The gaseous stream of component；
S2, is passed through the alkaline cleaner containing alkali lye by liquid phase stream and carries out alkali cleaning operation, polyethylene is separated out, catalyst
Inactivation, obtains mixture；
S3, the mixture is layered, and obtains being located at undermost alkali lye layer, the intermediate layer containing polyethylene
And the reaction liquid layer of the superiors.
According to the method that provides of the present invention, in the reaction liquid layer of the superiors, catalyst and contain with polymer
Amount is considerably less, and the clearance of catalyst is high (up to more than 97%), and the clearance of polyethylene is high (up to 98%).
The reaction liquid layer of the superiors can be passed through follow-up separator, isolate product, such as 1- hexenes, such as 1-
Octene etc..
According to a preferred embodiment of the present invention, ethylene oligomerization is produced in alpha-olefin technique, the reaction production
Thing includes ethene, solvent, catalyst, alpha-olefin and the polyethylene as accessory substance.Alpha-olefin is in the art
It is known, such as butylene, hexene, octene.Wherein, in an instantiation, the catalyst includes
Phenanthroline iron complex major catalyst and auxiliary agent containing aluminium.The solvent is solvent conventional in the art, preferably
For toluene and/or dimethylbenzene.According to the difference of specific process parameter, the amount of each component has difference in reaction product.
In a specific example, in the reaction product, the amount of polymer is 1.0-2.0wt%, such as from about 1.5wt
%.The auxiliary agent containing aluminium such as triethyl aluminum etc., content is calculated as 250ppm-500ppm with aluminium, based on reaction production
The quality of thing is basic to calculate.The catalyst
According to a preferred embodiment of the present invention, in step sl, the operating parameter of the flash distillation is as follows：
Pressure is 3.0-3.5Mpa, and temperature is 100-120 DEG C.By flash distillation, by gaseous stream and liquid containing light component
Phase logistics is separated.The light component contains ethene and butylene.The liquid phase stream is namely isolated and remained after light component
Under reaction solution.
According to a preferred embodiment of the present invention, in step s 2, operated by alkali cleaning, removal, which is helped, urges
Agent, prevents the generation of secondary response in reaction solution, it is ensured that the purity of product.Meanwhile, the condition of alkali cleaning is controlled,
Such as temperature, separates out ethylene oligomerization accessory substance polyethylene, otherwise polyethylene carries out follow-up point with reaction solution
From system, process pipelines are blocked.The temperature of the alkali cleaning is 50-100 DEG C, such as 50-90 DEG C.The alkali cleaning
Pressure is 0.2-0.3MPa.The residence time of the alkali cleaning is 20-60 minutes.The liquid phase stream and alkali lye
Mass ratio is 1:(0.5-2), such as 1:1.The alkali lye is 5-20wt%, the preferably alkali of 5-10wt% concentration
The aqueous solution.Wherein, preferably described alkali is selected from sodium hydroxide and potassium hydroxide.It is above-mentioned preferably under conditions of, energy
Access more preferable effect.In a specific embodiment, under agitation, mixed.
According to a preferred embodiment of the present invention, in the step S3, the operating parameter of the layering
It is as follows：Residence time 20-60 minute；And/or, operating pressure is 0.2-0.3Mpa；And/or, temperature control
At 50-100 DEG C.It is different with alkali lye density using reaction solution, polymer, by layering, reaction solution in the superiors,
Polyethylene is in intermediate layer, and alkali lye layer is in orlop.In the reaction solution containing solvent and heavy constituent (such as 1- hexenes,
1- octenes etc.) it is oil phase, positioned at the superiors.Phenanthroline iron complex in catalyst stays in intermediate layer, inhales
It is attached on polymer.Such as triethyl aluminum of auxiliary agent containing aluminium in catalyst, auxiliary agent containing aluminium reacts with alkali, the production of generation
Thing is also stayed in alkali lye layer.
According to a preferred embodiment of the present invention, the alkali lye layer in the step S3 is back in step S2
Alkaline cleaner, so as to be reused to alkali lye.Intermediate layer containing polymer is subjected to separation of solid and liquid, such as
Equipment for separating liquid from solid (such as filter) is passed through, the polymer of solid phase is obtained, liquid phase is back to alkaline cleaner, from
And alkali lye is reused.When carrying out circulation re-using to alkali lye, alkali lye and supplement can be periodically discharged
Fresh alkali lye, it is to avoid impurities accumulation.
According to another aspect of the present invention there is provided a kind of device for performing the above method, including：Perform
Step S1 flash tank, performs step S2 alkaline cleaner and performs step S3 layering tank, wherein,
Reaction product, which is passed through in flash tank, carries out flash separation, obtains liquid phase stream and the gaseous stream containing light component, so
Liquid phase stream, which is passed through in alkaline cleaner, afterwards obtains mixture, in alkaline cleaner, catalyst inactivation, and polyethylene
Separate out, mixture then is passed through into layering tank is layered, undermost alkali lye layer, the intermediate layer containing polyethylene
And the reaction liquid layer of the superiors.
According to device of the present invention preferred embodiment, described device further comprises separation of solid and liquid
Device, the intermediate layer containing polymer is passed through the equipment for separating liquid from solid and separated, and liquid phase is back to alkali cleaning
Device.Circulating pump can also be further comprised in described device, for undermost alkali lye to be recycled into alkaline cleaner.
According to the present invention, the alkaline cleaner, such as caustic treater or blender.The equipment for separating liquid from solid, such as mistake
Filter.
According to the present invention, what the catalysis for phenanthroline iron complex, triethyl aluminum, accelerator composition was catalyzed
Ethylene oligomerization produces alpha-olefin technique, and the polymer contained in product can be removed by the method in the application
And catalyst, it is to avoid cause process pipelines to block and influence the continuous operation of device, and avoid reaction solution
Secondary response and the generation for influenceing product quality.According to the present invention, without using conventional heat tracing technique, it is to avoid poly-
Compound enters follow-up workshop section with reaction solution, and and separation heavy constituent discharger together, so as to reduce energy
Consumption, it is to avoid cause the blocking of device.
The method provided according to the present invention, is carried out using the reaction solution to isolating the light components such as ethene and butylene
Alkali cleaning removes auxiliary agent containing aluminium, the generation of terminating reaction liquid secondary response, it is ensured that product purity；Pass through control simultaneously
Alkaline washes condition, and such as temperature separates out the ethylene oligomerization by-product polymer in reaction solution, utilizes reaction
Liquid, polymer are different with alkali cleaning density, and by layering, reaction solution is in the superiors, and polymer is in centre, alkali
Liquid separates polyethylene with the reaction solution containing product in orlop, prevents polyethylene blocking pipeline and sets
Standby and influence device operation steady in a long-term.Polyethylene is separated by equipment for separating liquid from solid (such as filter) again
Out, liquid phase also can return to alkaline cleaner, reduces cost and improves the utilization rate of alkali lye.The inventive method energy
Consumption it is smaller, and polymer (i.e. polyethylene) filtering not in logistic pipeline, do not interfere with the company of device
Reforwarding row.
Brief description of the drawings
Fig. 1 shows separation process figure according to an embodiment of the invention.
Embodiment
The present invention is with reference to the accompanying drawings and examples to be described further, but is not constituted to any of the present invention
Limitation.
Fig. 1 shows separation process figure according to an embodiment of the invention.Reaction product is left after reactor
The gaseous stream that flash tank flash separation obtains light component is directly entered, flash tank pressure is controlled in 3.0-3.5Mpa,
Temperature control is at 100-120 DEG C；Isolating the liquid phase stream after light component (also can be using mixing into caustic treater
Device) mixed with alkali lye, residence time 20-60 minute, alkaline cleaning procedure operating pressure is 0.2-0.3Mpa, alkali cleaning
Temperature control is at 50-100 DEG C.The mixed material of final reaction liquid and alkali lye enters layering tank layering, residence time
20-60 minutes, operating pressure was 0.2-0.3Mpa, and temperature control is at 50-100 DEG C.It is removing to be layered tank upper strata
Reaction solution after catalyst and polyethylene, subsequently into subsequent separation system；Centre is the layer containing polyethylene, is entered
Enter filter and filter out polyethylene, the liquid filtered out returns to caustic treater and reclaimed, lower floor's alkali lye is returned by circulating pump
Return caustic treater to recycle, while needing periodically discharge alkali lye and supplementing fresh alkali lye.It can thus remove anti-
Answer the polyethylene and catalyst (including auxiliary agent containing aluminium, such as triethyl aluminum) in liquid, it is to avoid the blocking of device and two
The generation of secondary response.Energy consumption of the present invention is smaller, and discharge of wastewater is also less.
In following examples, the major catalyst in catalyst used is chlorination 2- imido grpup -1,10- phenanthroline iron
(II), auxiliary agent containing aluminium is triethyl aluminum, and the mol ratio of auxiliary agent containing aluminium and major catalyst is calculated as 200 with aluminium/iron.
Embodiment 1：
Reaction product initially enters flash tank flash separation light component, and flash tank pressure is controlled in 3.5Mpa, temperature
Control is at 120 DEG C；Isolate the liquid phase stream after light component and enter caustic treater and alkali lye with stirring in mass ratio
1:1 mixing, 30 minutes residence times, alkaline cleaning procedure operating pressure be 0.3Mpa, alkali cleaning temperature control at 50 DEG C,
Alkali lye is the sodium hydrate aqueous solution of mass concentration 10%；The mixed material of final reaction liquid and alkali lye enters layering
Tank is layered, and 30 minutes residence times, operating pressure is 0.25Mpa, and temperature control is at 50 DEG C.It is layered on tank
Layer is reaction solution, into subsequent separation system；Intermediate layer contains polymer, and polymer is filtered out into filter,
The liquid filtered out returns to caustic treater and reclaimed；Lower floor's alkali lye returns to caustic treater by circulating pump and recycled.Specifically
Result of implementation is shown in Table 1.
Embodiment 2：
Reaction product initially enters flash tank flash separation light component, and flash tank pressure is controlled in 3.5Mpa, temperature
Control is at 120 DEG C.The liquid phase stream for isolating light component enters the caustic treater with stirring and alkali lye 1:1 mixing,
30 minutes residence times, alkaline cleaning procedure operating pressure is 0.3Mpa, and alkali cleaning temperature control is at 70 DEG C, and alkali lye is
The sodium hydrate aqueous solution of mass concentration 10%.The mixed material of final reaction liquid and alkali lye enters layering tank layering,
30 minutes residence times, operating pressure is 0.25Mpa, and temperature control is at 70 DEG C.It is reaction to be layered tank upper strata
Liquid, into subsequent separation system；Intermediate layer contains polymer, filters out polymer into filter, filters out
Liquid returns to caustic treater and reclaimed；Lower floor's alkali lye returns to caustic treater by circulating pump and recycled, and result is embodied
It is shown in Table 1.
Embodiment 3：
Reaction product initially enters flash tank flash separation light component, and flash tank pressure is controlled in 3.5Mpa, temperature
Control is at 120 DEG C.The liquid phase stream for isolating light component enters the caustic treater with stirring and alkali lye 1:1 mixing,
30 minutes residence times, alkaline cleaning procedure operating pressure is 0.3Mpa, and alkali cleaning temperature control is in 90 DEG C, alkali lye
For the sodium hydrate aqueous solution of mass concentration 10%.Final reaction liquid and alkali lye mixed material enter layering tank layering,
30 minutes residence times, operating pressure is 0.25Mpa, and temperature control is at 90 DEG C.It is reaction to be layered tank upper strata
Liquid, into subsequent separation system；Intermediate layer contains polymer, filters out polymer into filter, filters out
Liquid returns to caustic treater and reclaimed；Lower floor's alkali lye returns to caustic treater by circulating pump and recycled.Result is embodied
It is shown in Table 1.
Embodiment 4：
Reaction product initially enters flash tank flash separation light component, and flash tank pressure is controlled in 3.5Mpa, temperature
Control is at 120 DEG C.The liquid phase stream for isolating light component enters the caustic treater with stirring and alkali lye 1:1 mixing,
60 minutes residence times, alkaline cleaning procedure operating pressure is 0.3Mpa, and alkali cleaning temperature control is in 90 DEG C, alkali lye
For the sodium hydrate aqueous solution of mass concentration 10%.Final reaction liquid and alkali lye mixed material enter layering tank layering,
60 minutes residence times, operating pressure is 0.25Mpa, and temperature control is at 90 DEG C.It is reaction to be layered tank upper strata
Liquid, into subsequent separation system；Intermediate layer contains polymer, filters out polymer into filter, filters out
Liquid returns to caustic treater and reclaimed；Lower floor's alkali lye returns to caustic treater by circulating pump and recycled.Result is embodied
It is shown in Table 1.
Table 1
The data in table 1 are it is known that the method and apparatus provided according to the present invention, can effectively remove catalysis
Agent and polymer (i.e. polyethylene), clearance is all very high.The clearance of polymer content up to 98wt%,
And the clearance of catalyst is more than 97%.The method provided according to the present invention, flow is simple, energy consumption is small, energy
It is enough effectively to remove catalyst and polymer, prevent polyethylene blocking pipeline and equipment and influence the long-term steady of device
Fixed operation, and do not interfere with the continuous operation of device.Meanwhile, it is capable to terminate the generation of secondary response, it is ensured that production
Product purity.The method and apparatus provided according to the present invention, with broad application prospect.
It should be noted that embodiment described above is only used for explaining the present invention, do not constitute to the present invention's
Any limitation.By referring to exemplary embodiments, invention has been described, it should be appreciated that wherein used
Word is descriptive and explanatory vocabulary, rather than limited vocabulary.Can be by regulation in the claims in the present invention
In the range of the present invention is modified, and in without departing substantially from scope and spirit of the present invention to the present invention progress
Revision.Although the present invention described in it is related to specific method, material and embodiment, it is not intended that
The present invention is limited to wherein disclosed particular case, on the contrary, to can be extended to other all with identical function by the present invention
Methods and applications.
Claims (10)
1. removing the method for catalyst and polyethylene in a kind of ethylene oligomerization production alpha-olefin technique, comprise the following steps：
S1. the reaction product for ethylene oligomerization being produced into alpha-olefin carries out flash separation, obtains liquid phase stream and the gaseous stream containing light component；
S2, is passed through the alkaline cleaner containing alkali lye by liquid phase stream and carries out alkali cleaning operation, polyethylene is separated out, and catalyst inactivation obtains mixture；
S3, the mixture is layered, and obtains being located at undermost alkali lye layer, the intermediate layer containing polyethylene and the reaction liquid layer of the superiors.
2. according to the method described in claim 1, it is characterised in that the alkali cleaning operating condition is as follows：Temperature is 50-100 DEG C；And/or, pressure is 0.2-0.3MPa；And/or, the residence time is 20-60 minutes, or alkali cleaning operation is carried out under agitation.
3. method according to claim 1 or 2, it is characterised in that the mass ratio of the liquid phase stream and alkali lye is 1:(0.5-2)；And/or, the alkali lye is 5-20wt%, the preferably alkali of 5-10wt% the concentration aqueous solution, wherein, preferably described alkali is selected from sodium hydroxide and potassium hydroxide.
4. the method according to any one in claim 1-3, it is characterised in that the operating parameter of the flash distillation is as follows：Pressure is 3.0-3.5Mpa, and temperature is 100-120 DEG C.
5. the method according to any one in claim 1-4, it is characterised in that the operating parameter of the layering is as follows：Residence time 20-60 minute；And/or, operating pressure is 0.2-0.3Mpa；And/or, temperature control is at 50-100 DEG C.
6. the method according to any one in claim 1-5, it is characterised in that the alkali lye layer in the step S3 is back to the alkaline cleaner in step S2, and/or,
The intermediate layer containing polymer in the step S3 carries out separation of solid and liquid, obtains the polymer of solid phase, the liquid phase after separation is back to alkaline cleaner.
7. the method according to any one in claim 1-6, it is characterised in that in the ethylene oligomerization production alpha-olefin technique, the reaction product includes ethene, solvent, catalyst, alpha-olefin and the polyethylene as accessory substance；The solvent is preferably toluene and/or dimethylbenzene.
8. the method according to any one in claim 1-7, it is characterised in that the catalyst includes phenanthroline iron complex major catalyst and auxiliary agent containing aluminium.
9. a kind of perform claim requires the device of any one methods described in 1-8, including：Perform step S1 flash tank, perform step S2 alkaline cleaner and perform step S3 layering tank, wherein, reaction product, which is passed through in flash tank, carries out flash separation, obtains liquid phase stream and the gaseous stream containing light component, then liquid phase stream, which is passed through in alkaline cleaner, obtains mixture, in alkaline cleaner, catalyst inactivation, and polyethylene precipitation, then mixture is passed through into layering tank to be layered, undermost alkali lye layer, the intermediate layer containing polyethylene and the reaction liquid layer of the superiors.
10. device according to claim 9, it is characterised in that described device further comprises equipment for separating liquid from solid, the intermediate layer containing polymer is passed through the equipment for separating liquid from solid and separated, and liquid phase is back to alkaline cleaner；And/or, described device includes circulating pump, for undermost alkali lye to be recycled into alkaline cleaner.
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Cited By (4)
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| CN112745179A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method for producing alpha-olefin by ethylene oligomerization |
| CN112745185A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method for continuously producing alpha-olefin by ethylene oligomerization |
| CN114432985A (en) * | 2022-02-18 | 2022-05-06 | 内蒙古恒星化学有限公司 | Method and system for discharging waste alkali liquor in organic silicon production |
| CN115253967A (en) * | 2022-07-26 | 2022-11-01 | 山东京博石油化工有限公司 | Continuous ethylene selective oligomerization device and method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112745179A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method for producing alpha-olefin by ethylene oligomerization |
| CN112745185A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method for continuously producing alpha-olefin by ethylene oligomerization |
| CN114432985A (en) * | 2022-02-18 | 2022-05-06 | 内蒙古恒星化学有限公司 | Method and system for discharging waste alkali liquor in organic silicon production |
| CN115253967A (en) * | 2022-07-26 | 2022-11-01 | 山东京博石油化工有限公司 | Continuous ethylene selective oligomerization device and method |
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Application publication date: 20170912 |