CN106608790A - Method for production of ethylene through selective hydrogenation of acetylene - Google Patents
Method for production of ethylene through selective hydrogenation of acetylene Download PDFInfo
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- CN106608790A CN106608790A CN201510695773.0A CN201510695773A CN106608790A CN 106608790 A CN106608790 A CN 106608790A CN 201510695773 A CN201510695773 A CN 201510695773A CN 106608790 A CN106608790 A CN 106608790A
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- acetylene
- selective hydrogenation
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- ethylene
- hydrogenation
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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
The invention relates to a method for production of ethylene through selective hydrogenation of acetylene, wherein the method includes the steps: allowing acetylene dissolved in a solvent to enter a selective hydrogenation reactor in a liquid state, under a condition of selective hydrogenation, making acetylene contact with hydrogen gas and an acetylene selective hydrogenation catalyst, carrying out selective hydrogenation of acetylene, and converting into ethylene, wherein the solvent contains one or more of C4-C9 alkane, C4-C9 monoolefin, C4-C9 cycloolefin and C6-C8 aromatic hydrocarbons. The method for production of ethylene through selective hydrogenation of acetylene can effectively improve the selectivity of the catalyst and prolongs the service life of the catalyst while ensuring the acetylene conversion rate.
Description
Technical field
The present invention relates to a kind of method that acetylene selective hydrogenation produces ethylene.
Background technology
Ethylene is one of most important basic material of petrochemical industry, mainly passes through petroleum hydrocarbon steam splitting process
Production.Cracker produce cracking gas be by hydrogen, methane, C2 fractions, C3 fractions, C 4 fraction,
The mixture of the composition such as C 5 fraction and drippolene.Second containing 0.1%-0.5% (mole) in cracking gas
Alkynes, it is harmful for the reaction such as follow-up polymerization, therefore, in ethylene production flow process, generally make
Selective catalytic hydrogenation method is used, alkyne concentration is removed to into very low level (molar fraction<1×10-6),
To meet the requirement of polymer raw；The yield of ethylene can also be increased simultaneously, resource utilization is improved.
Acetylene chemistry industry once occupies an important position in basic organic chemical industry, but from last century 60
Since age, because petroleum hydrocarbon cracking obtains substantial amounts of cheap ethylene, propylene and with ethylene, propylene is
The exploitation of the various synthetic methods of raw material, in many organic synthesis fields, acetylene is progressively by ethylene and third
Alkene is replaced.Bulk product such as vinyl chloride, vinyl acetate, propylene of some past from acetylene manufacture
Cyanogen etc. is all had turned to ethylene, propylene as raw material, therefore, the demand of acetylene is gradually reduced.But,
With the development and the exploitation of shale gas of gas industry, the acetylene life with natural gas and shale gas as raw material
Production capacity power constantly expands, and the market supply ability of acetylene is gradually increasing.
To solve the imbalance between supply and demand of acetylene, with acetylene as raw material, by selecting hydrogenation second is converted the acetylene to
The method of alkene is increasingly taken seriously.Hydrogenation is selected with petroleum hydrocarbon steam splitting process production ethylene process
The method of removing acetylene is different, and the selection method of hydrotreating with acetylene as raw material has concentration of acetylene height, adds
Easily there is " temperature runaway " phenomenon in hydrogen, and catalyst surface can be tied because of high temperature and high concentration of acetylene
Close-burning carbon, causes catalyst to inactivate.Disadvantages mentioned above during to overcome acetylene hydrogenation, researchers visit
Rope some new methods.
CN103044179A reports the side that a kind of acetylene liquid phase selective hydrogenation in slurry bed system prepares ethylene
Method, introduces in gas-solid catalysis system and has the deliquescent liquid phase solvent of high selection to acetylene, using liquid phase
Solvent realizes PROCESS COUPLING to the high selection dissolubility of acetylene, improves the selectivity of ethylene, by acetylene plus
Hydrogen reaction preparative separation goes out ethylene.But, back-mixing is serious during the pass continuous operation, it is impossible to avoid ethylene
Hydrogenation, causes ethylene selectivity to reduce；Simultaneously also there is the separation problem of catalyst fines and anti-in the method
The separation problem of the oligomer that should be generated.
CN102489225B proposes the slurry bed process and its device of a kind of producing ethylene with acetylene hydrogenation, institute
It is to add add catalyst after water in the reactor to state technique, is passed through noble gases and enters line replacement, is heated
Afterwards the gaseous mixture of acetylene and hydrogen carried out instead by reactor bottom Jing gas distributors into reactor again
Should, finally product is discharged with unreacted unstripped gas by reactor head, ethylene is obtained after separation,
Unreacting gas are again introduced into reactor and are reacted after mixing with unstripped gas.Because reaction gas can not be dissolved in
Water, therefore the hydrogenation effect of the technique and bad, yield of ethene is relatively low.
CN101402541B mentions the fluidized-bed process and device of a kind of producing ethylene with acetylene hydrogenation, the technique
Including the fluidisation that acetylene and hydrogen mixture are passed through the catalyst equipped with Jing reduction and catalyst diluent
Bed reactor, selective hydrogenation of acetylene generates ethylene, cooling medium is passed through reactor heat exchange component to move
Dereaction heat, isolated ethylene product.The technological reaction temperature is 100-400 DEG C, at this temperature,
It is inevitable to generate a large amount of " green oils ", easily cause rapid catalyst deactivation；Due to the addition of in catalyst
Diluent, increased the difficulty of the catalyst recycling of efflorescence.
To sum up, the method for being provided using prior art produces ethylene by acetylene selective hydrogenation, and ethylene is selected
Property increase, but improve limitation, it is relatively low to still suffer from ethylene selectivity during acetylene selective hydrogenation,
The shortcomings of catalyst easy in inactivation, complex procedures.
The content of the invention
It is relatively low to there is ethylene selectivity in the method for producing ethylene for prior art acetylene selective hydrogenation, catalysis
The defects such as agent easy in inactivation, complex procedures, the present invention provides a kind of new acetylene selective hydrogenation production ethylene
Method.The method of acetylene selective hydrogenation production ethylene provided by the present invention is effectively improved catalyst
Selectivity, and extend the service life of catalyst.
The present invention provides a kind of method that new acetylene selective hydrogenation produces ethylene, and the method includes：Will be molten
Selective hydrogenation reaction device is entered with liquid phase state in the acetylene of solvent, in the case where hydroconversion condition is selected, with hydrogen
With acetylene selective hydrogenation catalyst contact, it is ethylene that acetylene carries out selection hydro-conversion, and the solvent contains
The alkane of C4-C9, in the aromatic hydrocarbons of the monoolefine of C4-C9, the cycloolefin of C4-C9 and C6-C8
Plant or various.
The present inventor passes through to study discovery, and the acetylene for being dissolved in solvent is added with liquid phase state into selection
Hydrogen reactor, carries out selective hydrogenation reaction, can effectively improve selectivity of catalyst energy, and extends
The service life of catalyst.Speculate that reason may be：Acetylene is diluted using solvent, selection is reduced and is added
The concentration of acetylene of hydrogen reactor entrance, thus the temperature rise of reaction bed is reduced, effectively inhibit polymer
Generation and other side reactions generation；And the flushing action because of liquid phase solvent to catalyst surface, effectively
Polymer is inhibited to deposit on catalyst surface.Therefore, the technology can effectively solving prior art lack
Fall into.
The method that the acetylene selective hydrogenation that the present invention is provided produces ethylene, while operation is simplified, keeps away
Exempt from catalyst " temperature runaway ", be effectively improved selectivity of catalyst, extend the use of catalyst
Life-span, with preferable prospects for commercial application.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute the part of description, with
Detailed description below is used to explain the present invention together, but is not construed as limiting the invention.
In accompanying drawing：
Fig. 1 is the process flow diagram that acetylene selective hydrogenation produces ethylene in embodiment 2.
Specific embodiment
The specific embodiment of the present invention is described in detail below.It should be appreciated that this place is retouched
The specific embodiment stated is merely to illustrate and explains the present invention, is not limited to the present invention.
The invention provides a kind of method that acetylene selective hydrogenation produces ethylene, the method includes：To be dissolved in
The acetylene of solvent with liquid phase state enter selective hydrogenation reaction device, select hydroconversion condition under, with hydrogen and
Acetylene selective hydrogenation catalyst is contacted, and acetylene carries out selecting hydro-conversion to be ethylene, and the solvent contains
The alkane of C4-C9, in the aromatic hydrocarbons of the monoolefine of C4-C9, the cycloolefin of C4-C9 and C6-C8
Plant or various.
In the present invention, the alkane includes chain alkane and cycloalkane.
In the present invention, the monoolefine referred to containing the unsaturated open chain olefins of a C=C in molecule,
Its formula is CnH2n。
In the present invention, the cycloolefin refers to and comprises only a cycloaliphatic ring and contain on cycloaliphatic ring
The hydrocarbon of one C=C, its formula is CnH2n-2。
In accordance with the present invention it is preferred that, the solvent contain butane, pentane, hexane, C4 raffinates,
C4, C5 raffinate, hydrocracking gasoline, benzene,toluene,xylene and aromatic hydrocarbons raffinate after MTBE ethers
One or more in oil.
In accordance with the present invention it is preferred that, it is described be dissolved in acetylene in the acetylene of solvent molar content be
1%-30%, preferably 2%-15%.It is more beneficial for improving selectivity of catalyst using this optimal way,
Extend the service life of catalyst.
In accordance with the present invention it is preferred that, the acetylene of solvent that is dissolved in carries out selection hydrogenation under liquid phase state
Reaction.
In accordance with the present invention it is preferred that, the selective hydrogenation reaction device is fixed bed hydrogenation reactor.
In the present invention, the selective hydrogenation reaction device can be single fixed bed hydrogenation reactor, also may be used
Be two or more series connection fixed bed hydrogenation reactor.
, according to the invention it is preferred to each fixed bed hydrogenation reactor entrance need to allocate hydrogen into, it is preferable that every
Individual fixed bed hydrogenation reactor porch hydrogen is respectively 0.2-4 with the mol ratio of acetylene.
In accordance with the present invention it is preferred that, when the fixed bed hydrogenation reactor connected using two or more,
Cooler is set between the fixed bed hydrogenation reactor of each two series connection.Can be moved using this optimal way
The heat that per section of reaction is produced is walked, the inlet temperature of lower first stage reactor is reduced, the hydrogenation reaction of acetylene is made
Carry out at a lower temperature, reduce the generation of " green oil ", slow down the coking reaction of catalyst surface,
Extend catalyst activity cycle.
In accordance with the present invention it is preferred that, the fixed bed hydrogenation reactor is selected from heat-insulating bubbling bed reactor
And/or heat-insulating trickle bed reactor.
In the present invention, the selection hydroconversion condition can be carried out according to acetylene content in handled raw material
Appropriate selection, in order to avoid the generation of " green oil ", fixed bed hydrogenation reactor inlet temperature should not mistake
Height, the selection of reaction pressure should meet makes the hydrogenation reaction of acetylene carry out under liquid phase state.
Preferably, the reaction pressure of the selective hydrogenation reaction is 0.2-4MPa, more preferably
0.6-2.5MPa。
Preferably, the inlet temperature of the selective hydrogenation reaction is 20-80 DEG C, more preferably
30-60 DEG C,
Preferably, the liquid volume air speed of the selective hydrogenation reaction is 1-200h-1, more preferably
40-160h-1。
In the present invention, the acetylene selective hydrogenation catalyst can be used for acetylene choosing for this area is any
Select the catalyst of hydrogenation reaction.
In accordance with the present invention it is preferred that, the acetylene selective hydrogenation catalyst includes carrier and is supported on carrier
On main active component and help active component.
In accordance with the present invention it is preferred that, the support selected from alumina, silicon oxide, spinelle, titanium oxide,
One or more in Zinc Oxide, stannum oxide and molecular sieve.It is more beneficial for improving using this preferred vector
Selectivity of catalyst, extends the service life of catalyst.
In accordance with the present invention it is preferred that, the main active component element is in palladium, rhodium, platinum and nickel element
One or more, preferably palladium element.It is more beneficial for improving catalysis using this preferably main active component
The selectivity of agent, extends the service life of catalyst.
In accordance with the present invention it is preferred that, it is described help active component element in silver, lead and copper one
Plant or various, preferably silver element.Active component is preferably helped to be more beneficial for improving catalyst using this
Selectivity, extends the service life of catalyst.
In accordance with the present invention it is preferred that, the acetylene selective hydrogenation catalyst also contains auxiliary agent.
The auxiliary element is preferably selected from alkali metal, alkali earth metal, transition metal, dilute
One or more in earth elements, VA races element and VIIA races element.
In the present invention, lutecium, scandium and yttrium are not included in the rare earth element.
In accordance with the present invention it is preferred that, the auxiliary element selected from potassium, sodium, lithium, calcium, magnesium, barium, fluorine,
One or more in gold, zinc, manganese, bismuth, molybdenum and zr element.
The implementation process and produced beneficial effect of the present invention are described in detail below by way of specific embodiment,
The spirit for being intended to help reader to more clearly understand the present invention is located, but can not be to the reality of the present invention
Apply scope and constitute any restriction.
Embodiment 1
Using single stage adiabatic fixed bed reactors, wherein filling 50mL palladium-silver selective hydrogenation catalysts (are carried
Body is aluminium oxide, and metal component content is：Weight % of palladium 0.3, silver-colored 0.1 weight %), by acetylene mole
Content is that 5.24% acetylene-hexane solution is matched somebody with somebody after hydrogen into reactor and catalyst haptoreaction, reacts bar
Part includes：Liquid volume air speed is 40h-1, reactor inlet hydrogen is 1.30 with the mol ratio of acetylene, instead
Device inlet temperature is answered for 36 DEG C, pressure is 0.82MPa.After reaction 4 hours, from single stage adiabatic fixed bed
It is 92.75% that reactor outlet sampling measures conversion of alkyne by chromatographic, ethylene selectivity
For 91.31%.After reaction 200 hours, from the outlet sampling of single stage adiabatic fixed bed reactors by gas phase color
It is 91.70% that spectrometer analysis measures conversion of alkyne, and ethylene selectivity is 90.31%.
Embodiment 2
Using double sections of insulation fix bed reactors, as shown in figure 1, first stage reactor I and second stage reactor
II loads respectively 50mL palladium-silver selective hydrogenation catalysts, and (carrier is aluminium oxide, and metal component content is：
Weight % of palladium 0.3, silver-colored 0.1 weight %), by acetylene-hexane solution (figure that acetylene molar content is 9.21%
Material flow A in 1) with first stage reactor I and catalyst haptoreaction is entered after hydrogen, first stage reactor I goes out
Mouthful logistics enters Jing after with hydrogen second stage reactor II and catalyst haptoreaction Jing after the cooling of cooler III, and one
The section reaction condition of reactor I includes：Liquid volume air speed is 80h-1, reactor inlet hydrogen and acetylene
Mol ratio is 0.7, and reactor inlet temperature is 38 DEG C, and pressure is 0.82MPa, and second stage reactor II is anti-
Condition is answered to include：Liquid volume air speed is 80h-1, reactor inlet hydrogen is 1.2 with the mol ratio of acetylene,
Reactor inlet temperature is 38 DEG C, and pressure is 0.78MPa.After reaction 4 hours, second stage reactor II goes out
Mouth logistics enters aftertreatment device knockout drum V Jing after the cooling of cooler IV.Second stage reactor II goes out
It is 96.12% that mouth sampling measures conversion of alkyne by chromatographic, and ethylene selectivity is 89.97%,
After reaction 200 hours, conversion of alkyne is measured by chromatographic from second stage reactor outlet sampling
For 95.32%, ethylene selectivity is 88.60%.
Embodiment 3
Using single stage adiabatic fixed bed reactors, wherein filling 50mL palladium-silver selective hydrogenation catalysts (are carried
Body is aluminium oxide, and metal component content is：Weight % of palladium 0.3, silver-colored 0.3 weight %, weight % of sodium 0.26),
Reaction raw materials are produced the mixture of the raffinate of carbon four by acetylene and butadiene product equipment, and it is specifically comprised：Second
Alkynes 3.27mol%, normal butane 10.66mol%, iso-butane 4.53mol%, 1-butylene 24.84mol%,
2-butylene 14.33mol%, isobutene. 42.07mol%, 1,3-butadiene<30 μ g/g, the 0.3mol% of carbon five.
By the raffinate liquor of acetylene-carbon four that acetylene molar content is 3.27% with enter after hydrogen reactor with
Catalyst haptoreaction, reaction condition includes：Liquid volume air speed is 100h-1, reactor inlet hydrogen
It is 1.33 with the mol ratio of acetylene, reactor inlet temperature is 42 DEG C, and pressure is 1.60MPa.Reaction 4
After hour, acetylene conversion is measured by chromatographic from single stage adiabatic fixed bed reactors outlet sampling
Rate is 94.63%, and ethylene selectivity is 90.09%.After reaction 200 hours, from single stage adiabatic fixed bed
It is 92.69% that reactor outlet sampling measures conversion of alkyne by chromatographic, ethylene selectivity
For 88.65%.
The acetylene selective hydrogenation life of present invention offer can be seen that by embodiment 1 to the data of embodiment 3
Ethylene method is produced, not only the conversion ratio of acetylene is higher, while improve the selectivity of ethylene, also, prolongs
Long response time, catalyst performance only has faint decline, the acetylene selective hydrogenation production second that the present invention is provided
Alkene method effectively extends the service life of catalyst.Therefore, acetylene selective hydrogenation provided by the present invention
The method of production ethylene has the incomparable superiority of existing additive method.
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, can be to the technical side of the present invention
Case carries out various simple variants, and these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique described in above-mentioned specific embodiment is special
Levy, in the case of reconcilable, can be combined by any suitable means.In order to avoid need not
The repetition wanted, the present invention is no longer separately illustrated to various possible compound modes.
Additionally, combination in any can also be carried out between a variety of embodiments of the present invention, as long as its
Without prejudice to the thought of the present invention, it should equally be considered as content disclosed in this invention.
Claims (11)
1. a kind of method that acetylene selective hydrogenation produces ethylene, it is characterised in that the method includes：Will
The acetylene for being dissolved in solvent enters selective hydrogenation reaction device with liquid phase state, in the case where hydroconversion condition is selected, with hydrogen
Gas and acetylene selective hydrogenation catalyst are contacted, and acetylene carries out selecting hydro-conversion to be ethylene, and the solvent contains
There is the alkane of C4-C9, in the aromatic hydrocarbons of the monoolefine of C4-C9, the cycloolefin of C4-C9 and C6-C8
One or more.
2. method according to claim 1, wherein, the solvent contain butane, pentane, oneself
C4, C5 raffinate after alkane, C4 raffinates, MTBE ethers, hydrocracking gasoline, benzene, toluene, two
One or more in toluene and Aromatic raffinate.
3. method according to claim 1 and 2, wherein, it is dissolved in acetylene in the acetylene of solvent
Molar content is 1%-30%, preferably 2%-15%.
4. the method according to any one in claim 1-3, wherein, the solvent that is dissolved in
Acetylene carries out selective hydrogenation reaction under liquid phase state.
5. the method according to any one in claim 1-4, wherein, it is described to select hydrogenation anti-
Device is answered to be fixed bed hydrogenation reactor.
6. the method according to any one in claim 1-5, wherein, it is described to select hydrogenation anti-
Answer the fixed bed hydrogenation reactor that device is single fixed bed hydrogenation reactor or two or more series connection, each institute
State fixed bed hydrogenation reactor porch hydrogen and be respectively 0.2-4 with the mol ratio of acetylene.
7. method according to claim 6, when the fixed bed hydrogenation connected using two or more it is anti-
When answering device, cooler is set between the fixed bed hydrogenation reactor of each two series connection.
8. the method according to any one in claim 5-7, wherein, the fixed bed hydrogenation
Reactor is selected from heat-insulating bubbling bed reactor and/or heat-insulating trickle bed reactor.
9. the method according to any one in claim 1-8, wherein, it is described to select hydrogenation bar
Part includes：Reaction pressure is 0.2-4MPa, preferably 0.6-2.5MPa；Inlet temperature is 20-80 DEG C,
Preferably 30-60 DEG C；Liquid volume air speed is 1-200h-1, preferably 40-160h-1。
10. the method according to any one in claim 1-9, wherein, the acetylene select plus
Hydrogen catalyst includes carrier and the main active component being supported on carrier and helps active component, the carrier choosing
One kind in self-alumina, silicon oxide, spinelle, titanium oxide, Zinc Oxide, stannum oxide and molecular sieve or
It is various；The main active component element is selected from one or more in palladium, rhodium, platinum and nickel element, preferably
For palladium element；Active component element is helped in silver, lead and copper one or more, preferably
For silver element.
11. methods according to claim 1 or 10, wherein, the acetylene selective hydrogenation catalysis
Agent also contains auxiliary agent, and the auxiliary element is selected from alkali metal, alkali earth metal, transition metal unit
One or more in element, rare earth element, VA races element and VIIA races element, is preferably selected from
One kind or many in potassium, sodium, lithium, calcium, magnesium, barium, fluorine, gold, zinc, manganese, bismuth, molybdenum and zr element
Kind.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107987011A (en) * | 2017-12-12 | 2018-05-04 | 安徽国星生物化学有限公司 | A kind of piperidines is continuously synthesizing to method |
| CN109518067A (en) * | 2017-09-19 | 2019-03-26 | 北京中联电科技术有限公司 | A kind of heavy oil catalytic cracking alloy and its application |
| CN111889035A (en) * | 2020-07-31 | 2020-11-06 | 山东京博中聚新材料有限公司 | Continuous hydrogenation production device and production method for carbon-carbon double bonds in unsaturated polymer |
| CN115178263A (en) * | 2021-04-07 | 2022-10-14 | 中国石油化工股份有限公司 | Catalyst for converting alkyne into olefin and preparation method and application thereof |
| CN115178264A (en) * | 2021-04-07 | 2022-10-14 | 中国石油化工股份有限公司 | Hydrogenation catalyst, preparation method and application thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4128595A (en) * | 1977-05-02 | 1978-12-05 | Phillips Petroleum Company | Acetylene hydrogenation in liquid phase with a liquid hydrocarbon reaction medium |
| US4571442A (en) * | 1983-09-19 | 1986-02-18 | Institut Francais Du Petrole | Process for selectively hydrogenating acetylene in a mixture of acetylene and ethylene |
| US20040176652A1 (en) * | 2003-03-04 | 2004-09-09 | Michel Molinier | Dual bed process using two different catalysts for selective hydrogenation of acetylene and dienes |
| CN101139242A (en) * | 2006-09-07 | 2008-03-12 | 中国石油化工股份有限公司 | Method for liquid phase selective hydrogenation of C3 hydrocarbons |
| CN101151227A (en) * | 2005-04-06 | 2008-03-26 | 沙特基础工业公司 | Method for selective hydrogenation of acetylene to ethylene |
| CN103044179A (en) * | 2012-12-19 | 2013-04-17 | 清华大学 | Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor |
| WO2016195954A1 (en) * | 2015-05-29 | 2016-12-08 | Uop Llc | Process for the selective hydrogenation of acetylene to ethylene |
-
2015
- 2015-10-23 CN CN201510695773.0A patent/CN106608790B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4128595A (en) * | 1977-05-02 | 1978-12-05 | Phillips Petroleum Company | Acetylene hydrogenation in liquid phase with a liquid hydrocarbon reaction medium |
| US4571442A (en) * | 1983-09-19 | 1986-02-18 | Institut Francais Du Petrole | Process for selectively hydrogenating acetylene in a mixture of acetylene and ethylene |
| US20040176652A1 (en) * | 2003-03-04 | 2004-09-09 | Michel Molinier | Dual bed process using two different catalysts for selective hydrogenation of acetylene and dienes |
| CN101151227A (en) * | 2005-04-06 | 2008-03-26 | 沙特基础工业公司 | Method for selective hydrogenation of acetylene to ethylene |
| CN101139242A (en) * | 2006-09-07 | 2008-03-12 | 中国石油化工股份有限公司 | Method for liquid phase selective hydrogenation of C3 hydrocarbons |
| CN103044179A (en) * | 2012-12-19 | 2013-04-17 | 清华大学 | Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor |
| WO2016195954A1 (en) * | 2015-05-29 | 2016-12-08 | Uop Llc | Process for the selective hydrogenation of acetylene to ethylene |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109518067A (en) * | 2017-09-19 | 2019-03-26 | 北京中联电科技术有限公司 | A kind of heavy oil catalytic cracking alloy and its application |
| CN107987011A (en) * | 2017-12-12 | 2018-05-04 | 安徽国星生物化学有限公司 | A kind of piperidines is continuously synthesizing to method |
| CN111889035A (en) * | 2020-07-31 | 2020-11-06 | 山东京博中聚新材料有限公司 | Continuous hydrogenation production device and production method for carbon-carbon double bonds in unsaturated polymer |
| CN115178263A (en) * | 2021-04-07 | 2022-10-14 | 中国石油化工股份有限公司 | Catalyst for converting alkyne into olefin and preparation method and application thereof |
| CN115178264A (en) * | 2021-04-07 | 2022-10-14 | 中国石油化工股份有限公司 | Hydrogenation catalyst, preparation method and application thereof |
| CN115178263B (en) * | 2021-04-07 | 2023-04-25 | 中国石油化工股份有限公司 | Catalyst for converting alkyne into alkene, preparation method and application thereof |
| CN115178264B (en) * | 2021-04-07 | 2023-04-25 | 中国石油化工股份有限公司 | Hydrogenation catalyst, preparation method and application thereof |
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| CN106608790B (en) | 2019-11-12 |
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