CN106608790B - A kind of method of acetylene selective hydrogenation production ethylene - Google Patents
A kind of method of acetylene selective hydrogenation production ethylene Download PDFInfo
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- CN106608790B CN106608790B CN201510695773.0A CN201510695773A CN106608790B CN 106608790 B CN106608790 B CN 106608790B CN 201510695773 A CN201510695773 A CN 201510695773A CN 106608790 B CN106608790 B CN 106608790B
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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
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- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The present invention relates to a kind of methods of acetylene selective hydrogenation production ethylene, this method comprises: the acetylene for being dissolved in solvent is entered selective hydrogenation reaction device with liquid phase state, in the case where selecting hydroconversion condition, it is contacted with hydrogen and acetylene selective hydrogenation catalyst, acetylene carries out selecting hydro-conversion for ethylene, the solvent contains the alkane of C4-C9, one of aromatic hydrocarbons of the monoolefine of C4-C9, the cycloolefin of C4-C9 and C6-C8 or a variety of.The method of acetylene selective hydrogenation production ethylene provided by the present invention effectively improves the selectivity of catalyst while guaranteeing conversion of alkyne, and extends the service life of catalyst.
Description
Technical field
The present invention relates to a kind of methods of acetylene selective hydrogenation production ethylene.
Background technique
Ethylene is one of most important basic material of petrochemical industry, is mainly produced by petroleum hydrocarbon steam splitting process.It splits
The cracking gas that solution device generates is made of mixed hydrogen, methane, C2 fraction, C3 fraction, C 4 fraction, C 5 fraction and drippolene etc.
Close object.In cracking gas contain 0.1%-0.5% (mole) acetylene, for it is subsequent polymerization etc. reactions be it is harmful, therefore,
In ethylene production process, usually using selective catalytic hydrogenation method, by alkyne concentration be removed to very low level (mole point
Number < 1 × 10-6), to meet the requirement of polymer raw；The yield of ethylene can also be increased simultaneously, improve resource utilization.
Acetylene chemistry industry once occupies an important position in basic organic chemical industry, but from the sixties in last century with
Come, since petroleum hydrocarbon cracking obtains a large amount of cheap ethylene, propylene and using ethylene, propylene as the various synthetic methods of raw material
Exploitation, in many organic synthesis fields, acetylene is gradually replaced ethylene and propylene.Some past are from acetylene manufacture
Bulk product such as vinyl chloride, vinyl acetate, propylene cyanogen etc. all has turned to using ethylene, propylene as raw material, therefore, the demand of acetylene
Amount is gradually reduced.But with the exploitation of the development of gas industry and shale gas, using natural gas and shale gas as the second of raw material
Alkynes production capacity constantly expands, and the market supply ability of acetylene is gradually increasing.
Pass through selection plus the hydrogen method that converts the acetylene to ethylene using acetylene as raw material for the imbalance between supply and demand for solving acetylene
Increasingly it is taken seriously.It is different from the selection method of hydrogenation and removing acetylene in petroleum hydrocarbon steam splitting process production ethylene process,
Using acetylene as the selection method of hydrotreating of raw material there is concentration of acetylene high plus hydrogen Yi Fasheng " temperature runaway " phenomenon, and catalyst table
Because of high temperature and high concentration of acetylene coking knot carbon can occur for face, cause catalyst inactivation.During overcoming acetylene hydrogenation
Disadvantages mentioned above, researchers explore some new methods.
CN103044179A reports a kind of method that acetylene liquid phase selective hydrogenation in slurry bed system prepares ethylene, in gas-solid
Introducing in catalyst system has the deliquescent liquid phase solvent of high selection to acetylene, is dissolved using high selection of the liquid phase solvent to acetylene
Property realize PROCESS COUPLING, improve the selectivity of ethylene, by acetylene hydrogenation react preparative separation go out ethylene.But the process connects
Back-mixing is serious when continuous operation, not can avoid ethylene hydrogenation, ethylene selectivity is caused to reduce；That there is also catalyst is thin for this method simultaneously
The separation problem for the oligomer that the separation problem of powder and reaction generate.
CN102489225B proposes the slurry bed process and its device of a kind of producing ethylene with acetylene hydrogenation, the technique be
Catalyst is added after water is added in reactor, inert gas is passed through and is replaced, again by the mixing of acetylene and hydrogen after heating
Gas enters reactor through gas distributor by reactor bottom and is reacted, finally by reaction product and unreacted unstripped gas by
Reactor head discharge, is made ethylene after separation, unreacting gas is again introduced into reactor after mixing with unstripped gas and is reacted.By
Water cannot be dissolved in reaction gas, thus the technique plus hydrogen effect and bad, yield of ethene is lower.
CN101402541B mentions the fluidized-bed process and device of a kind of producing ethylene with acetylene hydrogenation, which includes by acetylene
The fluidized-bed reactor equipped with the catalyst through restoring and catalyst diluent, selective hydrogenation of acetylene are passed through with hydrogen mixture
Ethylene is generated, cooling medium is passed through reactor heat exchange component to remove reaction heat, isolated ethylene product.The technological reaction
Temperature is 100-400 DEG C, at this temperature, inevitable to generate a large amount of " green oils ", easily causes rapid catalyst deactivation；Due to urging
It is added to diluent in agent, increases the difficulty of the catalyst recovery processing of dusting.
To sum up, ethylene is produced by acetylene selective hydrogenation using method provided by the prior art, ethylene selectivity is mentioned
Height, but improve limitation, lower, catalyst easy in inactivation that there are still ethylene selectivities during acetylene selective hydrogenation, process are multiple
The disadvantages of miscellaneous.
Summary of the invention
For the method for prior art acetylene selective hydrogenation production ethylene, that there are ethylene selectivities is lower, and catalyst is volatile
The defects of work, complex procedures, the present invention provide a kind of method of new acetylene selective hydrogenation production ethylene.It is provided by the present invention
The method of acetylene selective hydrogenation production ethylene effectively improves the selectivity of catalyst, and extends the use longevity of catalyst
Life.
The present invention provides a kind of method of new acetylene selective hydrogenation production ethylene, this method comprises: solvent will be dissolved in
Acetylene enters selective hydrogenation reaction device with liquid phase state, in the case where selecting hydroconversion condition, with hydrogen and acetylene selective hydrogenation catalyst
Contact, acetylene carries out selecting hydro-conversion for ethylene, and the solvent contains the alkane of C4-C9, the monoolefine of C4-C9, C4-C9
One of aromatic hydrocarbons of cycloolefin and C6-C8 is a variety of.
The present inventor passes through the study found that the acetylene for being dissolved in solvent enters selective hydrogenation reaction with liquid phase state
Device carries out selective hydrogenation reaction, can effectively improve the selection performance of catalyst, and extend the service life of catalyst.
Speculate that reason may are as follows: acetylene is diluted using solvent, reduces the concentration of acetylene of selective hydrogenation reaction device entrance, thus is reduced
The temperature rise of reaction bed effectively inhibits the generation of polymer and the generation of other side reactions；Again because liquid phase solvent is to catalyst
The flushing action on surface, effectively inhibits polymer to deposit on catalyst surface.Therefore, which can effectively solve existing skill
The defect of art.
The method of acetylene selective hydrogenation production ethylene provided by the invention avoids catalysis while simplifying process
Agent " temperature runaway ", effectively improves the selectivity of catalyst, extends the service life of catalyst, has preferable industrial application
Prospect.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the process flow diagram that acetylene selective hydrogenation produces ethylene in embodiment 2.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of methods of acetylene selective hydrogenation production ethylene, this method comprises: the second that will be dissolved in solvent
Alkynes enters selective hydrogenation reaction device with liquid phase state, in the case where selecting hydroconversion condition, connects with hydrogen and acetylene selective hydrogenation catalyst
Touching, acetylene carries out selecting hydro-conversion for ethylene, and the solvent contains the alkane of C4-C9, the list of the monoolefine of C4-C9, C4-C9
One of aromatic hydrocarbons of cycloolefin and C6-C8 is a variety of.
In the present invention, the alkane includes chain alkane and cycloalkane.
In the present invention, the monoolefine refers to the unsaturated open chain olefins containing a C=C in molecule, and general formula is
CnH2n。
In the present invention, the cycloolefin, which refers to, contains only a cycloaliphatic ring and contains a C=C on cycloaliphatic ring
Hydrocarbon, general formula CnH2n-2。
In accordance with the present invention it is preferred that C4, C5 take out after the solvent contains butane, pentane, hexane, C4 raffinate, MTBE ether
One of extraction raffinate, hydrocracking gasoline, benzene,toluene,xylene and Aromatic raffinate are a variety of.
In accordance with the present invention it is preferred that the molar content for being dissolved in acetylene in the acetylene of solvent is 1%-30%, preferably
2%-15%.It is more advantageous to the selectivity for improving catalyst using this preferred embodiment, extends the service life of catalyst.
In accordance with the present invention it is preferred that the acetylene for being dissolved in solvent carries out selective hydrogenation reaction under liquid phase state.
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, be also possible to two
The above concatenated fixed bed hydrogenation reactor.
, according to the invention it is preferred to which each fixed bed hydrogenation reactor entrance need to be incorporated hydrogen, it is preferable that each fixed bed adds
The molar ratio of hydrogen reactor inlet hydrogen and acetylene is respectively 0.2-4.
In accordance with the present invention it is preferred that connecting when using more than two concatenated fixed bed hydrogenation reactors in every two
Fixed bed hydrogenation reactor between cooler is set.The heat that every section of reaction generates can be removed using this preferred embodiment,
The inlet temperature for reducing lower first stage reactor, carries out the hydrogenation reaction of acetylene at a lower temperature, reduces the life of " green oil "
At the coking for slowing down catalyst surface is reacted, and catalyst activity cycle is extended.
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 insulation
Formula trickle bed reactor.
In the present invention, the selection hydroconversion condition can carry out choosing appropriate according to acetylene content in handled raw material
It selects, in order to avoid the generation of " green oil ", fixed bed hydrogenation reactor inlet temperature is unsuitable excessively high, and the selection of reaction pressure should meet
Carry out the hydrogenation reaction of acetylene under liquid phase state.
Preferably, the reaction pressure of the selective hydrogenation reaction is 0.2-4MPa, further preferably 0.6-2.5MPa.
Preferably, the inlet temperature of the selective hydrogenation reaction be 20-80 DEG C, further preferably 30-60 DEG C,
Preferably, the liquid volume air speed of the selective hydrogenation reaction is 1-200h-1, further preferably 40-160h-1。
In the present invention, the acetylene selective hydrogenation catalyst can any to can be used for acetylene selective hydrogenation anti-for this field
The catalyst answered.
In accordance with the present invention it is preferred that the acetylene selective hydrogenation catalyst includes carrier and the main work that is supported on carrier
Property component and help active component.
In accordance with the present invention it is preferred that the carrier is selected from aluminium oxide, silica, spinelle, titanium oxide, zinc oxide, oxidation
One of tin and molecular sieve are a variety of.It is more advantageous to the selectivity for improving catalyst using this preferred vector, extends catalysis
The service life of agent.
In accordance with the present invention it is preferred that the main active component element is selected from one of palladium, rhodium, platinum and nickel element or more
Kind, preferably palladium element.It is more advantageous to the selectivity for improving catalyst using this preferably main active component, extends catalyst
Service life.
In accordance with the present invention it is preferred that described help active component element to be selected from one of silver, lead and copper or a variety of,
Preferably silver element.Preferably active component is helped to be more advantageous to the selectivity of raising catalyst using this, extends making for catalyst
Use the service life.
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 element, alkali earth metal, transition metal element, rare earth element,
One of VA race element and V Group IIA element are a variety of.
It in the present invention, does not include lutetium, scandium and yttrium in the rare earth element.
In accordance with the present invention it is preferred that the auxiliary element is selected from potassium, sodium, lithium, calcium, magnesium, barium, fluorine, gold, zinc, manganese, bismuth, molybdenum
With one of zr element or a variety of.
Below by way of the specific embodiment implementation process that the present invention will be described in detail and generated beneficial effect, it is intended to help
Where reader more clearly understands Spirit Essence of the invention, but any restriction cannot be constituted to practical range of the invention.
Embodiment 1
Using single stage adiabatic fixed bed reactors, wherein filling 50mL palladium-silver selective hydrogenation catalyst (carrier is aluminium oxide,
Metal component content are as follows: 0.3 weight % of palladium, 0.1 weight % of silver), the acetylene-hexane solution for being 5.24% by acetylene molar content
With reactor and catalyst haptoreaction is entered after hydrogen, reaction condition includes: that liquid volume air speed is 40h-1, reactor inlet hydrogen
The molar ratio of gas and acetylene is 1.30, and reactor inlet temperature is 36 DEG C, pressure 0.82MPa.After reaction 4 hours, from single hop
It is 92.75% that insulation fix bed reactor outlet sampling, which measures conversion of alkyne by chromatographic, and ethylene selectivity is
91.31%.After reaction 200 hours, acetylene is measured from single stage adiabatic fixed bed reactors outlet sampling by chromatographic
Conversion ratio is 91.70%, ethylene selectivity 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 load respectively
50mL palladium-silver selective hydrogenation catalyst (carrier is aluminium oxide, metal component content are as follows: 0.3 weight % of palladium, 0.1 weight % of silver),
Enter first stage reactor I and catalysis after acetylene-hexane solution (material flow A in Fig. 1) that acetylene molar content is 9.21% is matched hydrogen
Agent haptoreaction, I outlet streams of first stage reactor enter second stage reactor II and catalysis after cooler III is cooling after with hydrogen
Agent haptoreaction, I reaction condition of first stage reactor include: that liquid volume air speed is 80h-1, reactor inlet hydrogen and acetylene
Molar ratio is 0.7, and reactor inlet temperature is 38 DEG C, pressure 0.82MPa, and II reaction condition of second stage reactor includes: liquid
Volume space velocity is 80h-1, the molar ratio of reactor inlet hydrogen and acetylene is 1.2, and reactor inlet temperature is 38 DEG C, and pressure is
0.78MPa.After reaction 4 hours, II outlet streams of second stage reactor enter aftertreatment device gas-liquid after cooler IV is cooling
Knockout drum V.It is 96.12% that the outlet of second stage reactor II sampling, which measures conversion of alkyne by chromatographic, ethylene selection
Property be 89.97%, after reaction 200 hours, conversion of alkyne measured by chromatographic from second stage reactor outlet sampling
It is 95.32%, ethylene selectivity 88.60%.
Embodiment 3
Using single stage adiabatic fixed bed reactors, wherein filling 50mL palladium-silver selective hydrogenation catalyst (carrier is aluminium oxide,
Metal component content are as follows: 0.3 weight % of palladium, silver 0.3 weight %, 0.26 weight % of sodium), reaction raw materials are that acetylene and butadiene fill
Set the mixture of produced four raffinate of carbon, concrete composition are as follows: acetylene 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, light dydrocarbon 0.3mol%.
It is connect into reactor with catalyst after acetylene molar content is matched hydrogen for 3.27% four raffinate liquor of acetylene-carbon
Touching reaction, reaction condition include: that liquid volume air speed is 100h-1, the molar ratio of reactor inlet hydrogen and acetylene is 1.33, instead
Answering device inlet temperature is 42 DEG C, pressure 1.60MPa.Reaction 4 hours after, from single stage adiabatic fixed bed reactors export sampling by
It is 94.63% that chromatographic, which measures conversion of alkyne, ethylene selectivity 90.09%.After reaction 200 hours, from list
It is 92.69% that the outlet sampling of section insulation fix bed reactor, which measures conversion of alkyne by chromatographic, ethylene selectivity
It is 88.65%.
The acetylene selective hydrogenation production provided by the invention ethylene side it can be seen from the data of embodiment 1 to embodiment 3
Method, not only the conversion ratio of acetylene is higher, while improving the selectivity of ethylene, also, extends the reaction time, and catalyst performance is only
There is faint decline, acetylene selective hydrogenation production ethylene method provided by the invention effectively extends the service life of catalyst.Cause
This, the method for acetylene selective hydrogenation provided by the present invention production ethylene has incomparable superior of existing other methods
Property.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, it can be combined in any appropriate way.In order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (9)
1. a kind of method of acetylene selective hydrogenation production ethylene, which is characterized in that this method comprises: by the acetylene for being dissolved in solvent with
Liquid phase state enters selective hydrogenation reaction device, in the case where selecting hydroconversion condition, contacts with hydrogen and acetylene selective hydrogenation catalyst, second
Alkynes carries out selecting hydro-conversion for ethylene, and the solvent contains the alkane of C4-C9, the monocycle alkene of the monoolefine of C4-C9, C4-C9
One of aromatic hydrocarbons of hydrocarbon and C6-C8 is a variety of, and the molar content for being dissolved in acetylene in the acetylene of solvent is 1%-30%, described molten
Selective hydrogenation reaction is carried out under liquid phase state in the acetylene of solvent；It is described that select hydroconversion condition include: reaction pressure for 0.6-
2.5MPa, inlet temperature are 30-60 DEG C；Liquid volume air speed is 40-160h-1；
The selective hydrogenation reaction device is more than two concatenated fixed bed hydrogenation reactors, is added in the concatenated fixed bed of every two
Cooler is set between hydrogen reactor, and the molar ratio of each fixed bed hydrogenation reactor inlet hydrogen and acetylene is respectively
0.2-4。
2. according to the method described in claim 1, wherein, the solvent contains butane, pentane, hexane, C4 raffinate, MTBE ether
One of C4, C5 raffinate, hydrocracking gasoline, benzene,toluene,xylene and Aromatic raffinate or a variety of afterwards.
3. according to the method described in claim 1, wherein, the molar content for being dissolved in acetylene in the acetylene of solvent is 2%-15%.
4. method described in any one of -3 according to claim 1, wherein the selective hydrogenation reaction device is fixed bed hydrogenation
Reactor.
5. according to the method described in claim 4, wherein, the fixed bed hydrogenation reactor is selected from heat-insulating bubbling bed reactor
And/or heat-insulating trickle bed reactor.
6. method described in any one of -3 according to claim 1, wherein the acetylene selective hydrogenation catalyst includes carrier
With the main active component that is supported on carrier and help active component, the carrier is selected from aluminium oxide, silica, spinelle, oxidation
One of titanium, zinc oxide, tin oxide and molecular sieve are a variety of；The main active component element is selected from palladium, rhodium, platinum and nickel element
One of or it is a variety of；It is described that active component element is helped to be selected from one of silver, lead and copper or a variety of.
7. according to the method described in claim 6, wherein, the main active component element is palladium element；It is described to help active component
Element is silver element.
8. according to the method described in claim 6, wherein, the acetylene selective hydrogenation catalyst also contains auxiliary agent, the auxiliary agent
Element is selected from alkali metal element, alkali earth metal, transition metal element, rare earth element, V A race's element and V Group IIA member
One of element is a variety of.
9. according to the method described in claim 8, wherein, the auxiliary element be selected from potassium, sodium, lithium, calcium, magnesium, barium, fluorine, gold,
One of zinc, manganese, bismuth, molybdenum and zr element are a variety of.
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| CN109518067B (en) * | 2017-09-19 | 2021-01-22 | 北京中联电科技术有限公司 | Heavy oil catalytic cracking alloy and application thereof |
| 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 |
| CN111889035B (en) * | 2020-07-31 | 2023-01-31 | 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 |
| 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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| US4571442A (en) * | 1983-09-19 | 1986-02-18 | Institut Francais Du Petrole | Process for selectively hydrogenating acetylene in a mixture of acetylene and ethylene |
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| 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 |
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| US7038097B2 (en) * | 2003-03-04 | 2006-05-02 | Exxonmobil Chemical Patents Inc. | Dual bed process using two different catalysts for selective hydrogenation of acetylene and dienes |
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| 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 |
| CN101151227A (en) * | 2005-04-06 | 2008-03-26 | 沙特基础工业公司 | Method for selective hydrogenation of acetylene to ethylene |
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