CN105967972A - Method for preparing benzene and co-producing ethylene from acetylene - Google Patents
Method for preparing benzene and co-producing ethylene from acetylene Download PDFInfo
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- CN105967972A CN105967972A CN201610306254.5A CN201610306254A CN105967972A CN 105967972 A CN105967972 A CN 105967972A CN 201610306254 A CN201610306254 A CN 201610306254A CN 105967972 A CN105967972 A CN 105967972A
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- acetylene
- benzene
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- unstripped gas
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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
- C07C2/42—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons homo- or co-oligomerisation with ring formation, not being a Diels-Alder conversion
- C07C2/48—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons homo- or co-oligomerisation with ring formation, not being a Diels-Alder conversion of only hydrocarbons containing a carbon-to-carbon triple bond
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
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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 discloses a method for preparing benzene and co-producing ethylene from acetylene. The method comprises the following steps: (1) mixing the acetylene, hydrogen, methane and steam to obtain feed gas; (2) supplying the feed gas to a reactor with a catalyst for reaction; (3) performing separation treatment on a material obtained by reaction in step (2) to obtain the benzene and the ethylene. According to the method, multiple reactions are coupled, so that the shortcomings of complexity in catalyst preparation, poor selectivity, harsh process conditions, high carbon deposition rate and requirements on use of a toxic solvent during alkyne aromatization reaction are overcome, the problem of high catalyst deactivation rate caused by heat transfer difficulty and high green oil production rate of a high-concentration acetylene hydrogenation process is solved, and the benzene and the ethylene can be prepared at the same time; moreover, the method has the advantages of simple process, easiness for temperature control and product selectivity adjustability, and is suitable for large-scale production.
Description
Technical field
The invention belongs to chemical technology field, specifically, the present invention relates to a kind of acetylene and prepare benzene and the method for coproduction ethylene.
Background technology
Benzene and ethylene are all important petrochemical materials, and product is widely used in environment, the energy, industry, life downstream
The fields such as thing.But, ethylene is mainly prepared by the method for cracking petroleum hydrocarbon, and benzene mainly extracts from oil product.China
The few gas of rich coal oil starvation, dependence on foreign countries for oil is high, and this defines serious war for China that oil reserve is not enriched
Slightly threaten.Therefore, seek another kind of new source and process prepares large basic chemical industry benzene feedstock and ethylene, in work
Industry production field petroleum replacing is as raw material, it is possible to largely alleviate China's dependency for oil.
Along with petroleum resources are the most exhausted, Development of Coal chemical industry is that the chemical process of raw material becomes the important of petroleum replacing chemical industry route
Process.In coal chemical technology, produce acetylene for raw material by carbide technique with coal, have been widely used, with acetylene as raw material
Preparation Elementary Chemical Industry raw material, can expand Coal Chemical Industry Route further.
Acetylene three is polymerized to the report of benzene can trace back to 1866, and Betholet finds acetylene hot conditions more than 400 DEG C
Under, it is possible to generate a small amount of trimerization product benzene.Reppe in 1948 etc. find transition metal-catalyzed alkynes ring trimerization generate benzene and
The reaction of its derivant, causes the extensive concern of people.Chemist finds that multiple transition metal is to alkynes ring three in recent years
Poly-have catalytic action.But all also exist that the easy carbon distribution of bed, catalyst preparation be complicated and easy in inactivation, selectivity are low, need to use
The defects such as toxic solvent.
The report of preparation of ethylene through selective hydrogenation of acetylene also compares many, but its research contents is mainly used in removing cracking petroleum hydrocarbon and prepares
The acetylene (0.01～5 volume %) of trace during ethylene process.Acetylene hydrogenation is strong exothermal reaction, and high concentration acetylene hydrogenation is released
A large amount of reaction heat, bed moves heat difficulty, easily causes catalysqt deactivation, side reaction increases, yield of ethene declines, so for
The rare exploration of method of the special catalysis selective hydrogenation ethylene with high concentration acetylene as raw material, corresponding industrialization on a large scale should
With having no report especially.
But, along with benzene and the wilderness demand of ethylene, how to utilize acetylene to prepare benzene simultaneously and ethylene becomes and needs solution at present badly
Problem.
Summary of the invention
It is contemplated that one of technical problem solved the most to a certain extent in correlation technique.To this end, the one of the present invention
Purpose is that proposing a kind of acetylene prepares benzene and the method for coproduction ethylene, and the method is by by multiple reaction couplings, solving existing
Have various problems present in technology, such as, it is to avoid catalyst preparation complexity in alkynes aromatization, poor selectivity,
Process conditions carbon distribution harsh, easy and need use toxic solvent defect；Overcome high concentration acetylene hydrogenation technique move heat difficulty,
Be easily generated green oil and cause the problem of catalysqt deactivation, such that it is able to prepare benzene and ethylene simultaneously, and have technique simple,
Easy temperature control system, the adjustable advantage of product selectivity, it is suitable for large-scale production.
In one aspect of the invention, the present invention proposes a kind of acetylene and prepares benzene and the method for coproduction ethylene.According to the present invention
Embodiment, described method includes:
(1) acetylene, hydrogen, methane and steam are mixed, in order to obtain unstripped gas；
(2) supply of described unstripped gas is reacted to the reactor be provided with catalyst；
(3) the reacted material that step (2) obtains is carried out separating treatment, in order to obtain benzene and ethylene.
Thus, acetylene according to embodiments of the present invention prepares the method for benzene and coproduction ethylene by by multiple reaction couplings, it is to avoid
In alkynes aromatization, catalyst preparation complexity, poor selectivity, process conditions carbon distribution harsh, easy and needing uses poisonous
The defect of solvent, overcomes high concentration acetylene hydrogenation technique simultaneously and moves heat difficulty, is easily generated green oil and causes asking of catalysqt deactivation
Topic, such that it is able to prepare benzene and ethylene simultaneously, and has that technique is simple, easy temperature control system, and product selectivity is adjustable
Advantage, be suitable for large-scale production.
Can also have following additional it addition, the method for benzene and coproduction ethylene prepared by acetylene according to the above embodiment of the present invention
Technical characteristic:
In some embodiments of the invention, in described unstripped gas, described acetylene, described hydrogen, the mol ratio of described methane
For 1:(1～3.5): (1～4), the content of described steam is 100～2000ppm, and described unstripped gas temperature not higher than 90 is taken the photograph
Family name's degree.Thus, it is possible to significantly improve the yield of benzene and ethylene.
In some embodiments of the invention, described unstripped gas farther includes other components, and other components described are selected from second
At least one in alkane, carbon dioxide and carbon monoxide, and each constituent content is not higher than 1000ppm.
In some embodiments of the invention, described catalyst comprises active component and carrier, and described active component is the VIIIth race
One or more in one or more in metal, or group VIII metal and silver, copper, titanium, gallium, molybdenum and indium are formed
Combination, wherein, the load capacity of described active component accounts for 0.01wt%～0.1wt% of described carrier.Thus, it is possible to carry further
High benzene and the yield of ethylene.
In some embodiments of the invention, described carrier is selected from SiO2、α-Al2O3、TiO2, glass fiber mesh and glass
At least one in pearl.Thus, it is possible to improve benzene and the yield of ethylene further.
In some embodiments of the invention, in step (2), the temperature of described reaction is 400～800 degrees Celsius, pressure
Not higher than 1.0MPa.Thus, it is possible to improve benzene and the yield of ethylene further.
In some embodiments of the invention, described reactor is fluid bed, moving bed or calandria type fixed bed, wherein, institute
State fluid bed air speed be 1000～50000ml/ (g cat h), described moving bed or described calandria type fixed bed air speed be 500～
5000h-1.Thus, it is possible to improve benzene and the yield of ethylene further.
In some embodiments of the invention, the reaction zone of described reactor is non-metallic material with the part of described feed gas
Matter, wherein, described non-metallic material is at least one in graphite, enamel, pottery and quartz.Thus, it is possible to enter
One step improves benzene and the yield of ethylene.
In some embodiments of the invention, described reaction mass farther includes ethane, butane, butylene, butadiene, second
In vinyl acetylene, divinylacetylene and cyclo-octatetraene at least one.
In some embodiments of the invention, the particle diameter of catalyst is 20-40 mesh.
The additional aspect of the present invention and advantage will part be given in the following description, and part will become bright from the following description
Aobvious, or recognized by the practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or the additional aspect of the present invention and advantage will be apparent from from combining the accompanying drawings below description to embodiment
With easy to understand, wherein:
Fig. 1 is the method flow schematic diagram that acetylene prepares benzene and coproduction ethylene according to an embodiment of the invention.
Detailed description of the invention
Embodiments of the invention are described below in detail, and the example of described embodiment is shown in the drawings, the most identical
Or similar label represents same or similar element or has the element of same or like function.Retouch below with reference to accompanying drawing
The embodiment stated is exemplary, it is intended to is used for explaining the present invention, and is not considered as limiting the invention.
In one aspect of the invention, the present invention proposes a kind of acetylene and prepares benzene and the method for coproduction ethylene.According to the present invention
Embodiment, the method includes: acetylene, hydrogen, methane and steam are mixed by (1), in order to obtain unstripped gas；
(2) supply of described unstripped gas is reacted to the reactor be provided with catalyst；(3) step (2) is reacted
After material carry out separating treatment, in order to obtain benzene and ethylene.Inventor finds, by by multiple reaction couplings, solving
Multiple problem of the prior art, such as, avoid catalyst preparation complexity, poor selectivity, technique in alkynes aromatization
Condition carbon distribution harsh, easy and need use toxic solvent defect；Overcome high concentration acetylene hydrogenation technique and move hot difficult, easily
Produce green oil and cause the problem of catalysqt deactivation, such that it is able to prepare benzene and ethylene simultaneously, and have technique simple,
Easy temperature control system, the adjustable advantage of product selectivity, it is suitable for large-scale production.
The method being prepared by the acetylene of the embodiment of the present invention benzene and coproduction ethylene below with reference to Fig. 1 is described in detail.According to this
Inventive embodiment, the method includes:
S100: acetylene, hydrogen, methane and steam are mixed
According to embodiments of the invention, acetylene, hydrogen, methane and steam are mixed, such that it is able to obtain unstripped gas.
According to one embodiment of present invention, in unstripped gas, acetylene, hydrogen, the mol ratio of methane can be 1:(1～3.5):
(1～4), the content of steam can be 100～2000ppm, and the temperature of unstripped gas is not higher than 90 degrees Celsius.
According to still a further embodiment, unstripped gas may further include other components, and wherein, other components are permissible
For at least one in ethane, carbon dioxide and carbon monoxide, and each constituent content can be not higher than 1000ppm.
S200: unstripped gas supply is reacted to the reactor be provided with catalyst
According to embodiments of the invention, anti-by above-mentioned mixing gained unstripped gas supply to the reactor be provided with catalyst is carried out
Should, such that it is able to obtain reaction mass.According to one embodiment of present invention, catalyst comprises active component and carrier, institute
Stating active component is one or more in group VIII metal, or in group VIII metal and silver, copper, titanium, gallium, molybdenum and indium
One or more combinations formed.
According to further embodiment of the present invention, the load capacity of the VIIIth metal accounts for 0.01wt%～0.1wt% of total weight of carrier
According to still another embodiment of the invention, carrier can be selected from SiO2、α-Al2O3、TiO2, glass fiber mesh and glass
At least one in glass pearl.
According to still another embodiment of the invention, the particle diameter of catalyst can be 20-40 mesh.
According to still another embodiment of the invention, the particular type of reactor is not particularly restricted, and those skilled in the art can
To select according to actual needs, according to a particular embodiment of the invention, reactor can be fluid bed, moving bed or row
Tubular fixed-bed.
A specific embodiment according to the present invention, when using fluid bed as reactor, fluid bed air speed can be
1000～50000ml/ (g cat h).
According to another specific embodiment of the present invention, when using moving bed as reactor, the air speed of moving bed can be
500～5000h-1。
According to another specific embodiment of the present invention, when use calandria type fixed bed as reactor time, calandria type fixed bed
Air speed can be 500～5000h-1。
According to still another embodiment of the invention, the reaction zone of reactor and the part of feed gas can be non-metallic material,
Wherein, non-metallic material is at least one in graphite, enamel, pottery and quartz.Another according to the present invention is real
Executing example, the reaction temperature in reactor can be 400～800 degrees Celsius, and pressure can be not higher than 1.0MPa.According to the present invention
Another embodiment, in this step obtained by reaction mass in may further include ethane, butane, butylene, fourth two
In alkene, vinylacetylene, divinylacetylene and cyclo-octatetraene at least one.
S300: reaction mass is carried out separating treatment
According to embodiments of the invention, the reaction mass obtained by above-mentioned is carried out separating treatment, such that it is able to obtain benzene and second
Alkene.
Acetylene according to embodiments of the present invention prepares the method for benzene and coproduction ethylene by by multiple reaction couplings, solving existing
Multiple problems present in technology, such as, it is to avoid catalyst preparation complexity, poor selectivity, work in alkynes aromatization
Skill condition carbon distribution harsh, easy and need to use the defect of toxic solvent, overcome high concentration acetylene hydrogenation technique to move heat tired simultaneously
Difficult, be easily generated green oil and cause the problem of catalysqt deactivation, such that it is able to prepare benzene and ethylene simultaneously, and there is technique
Simply, easy temperature control system, the adjustable advantage of product selectivity, be suitable for large-scale production.
Below with reference to specific embodiment, present invention is described, it should be noted that these embodiments are the most descriptive
, and limit the present invention never in any form.
Embodiment 1
Acetylene, hydrogen, methane, steam and carbon dioxide are mixed, obtains unstripped gas, wherein, second in unstripped gas
Alkynes is 1:3:2 with hydrogen and methane mol ratio, and in unstripped gas, water vapour content is 100～2000ppm, and carbon dioxide is
1000ppm；Unstripped gas is all pressed as 0.75MPa, and unstripped gas temperature is 35 DEG C, then supplies unstripped gas to being filled with catalysis
Agent calandria type fixed bed in, and calandria type fixed bed in be enamel material, wherein, catalyst with feed gas part
Being prepared from by infusion process, particle diameter is 20～40 mesh, and active component is palladium, copper and nickel, and load capacity is the 0.05wt% of carrier,
Catalyst carrier is glass fiber mesh, and reactor operation air speed is 3000h-1, reaction temperature is to react at 450 DEG C,
To the reaction mass containing benzene, ethylene, ethane, butane, butylene, butadiene, vinylacetylene and cyclo-octatetraene, then
Reaction mass is carried out separating treatment, it is hereby achieved that benzene and ethylene.
Embodiment 2
Acetylene, hydrogen, methane, steam and carbon dioxide are mixed, obtains unstripped gas, wherein, second in unstripped gas
Alkynes is 1:1:4 with hydrogen and methane mol ratio, and in unstripped gas, water vapour content is 1000ppm, and carbon dioxide is 500ppm,；
Unstripped gas is all pressed as 0.55MPa, unstripped gas temperature 80 DEG C, then by unstripped gas supply to the moving bed being filled with catalyst,
And being ceramic material with feed gas part in moving bed, wherein, catalyst is prepared from by infusion process, and particle diameter is
5～8mm, activity component metal is palladium, copper, ferrum and nickel, and load capacity is the 0.04wt% of carrier, and catalyst carrier is α-Al2O3,
Reactor operation air speed is 2000h-1, reaction temperature is to react at 650 DEG C, obtains containing benzene, ethylene, ethane, fourth
Alkene, butadiene, vinylacetylene, divinylacetylene, the reaction mass of cyclo-octatetraene, then carried out reaction mass point
From process, it is hereby achieved that benzene and ethylene.
Embodiment 3
Acetylene, hydrogen, methane, steam and carbon dioxide, carbon monoxide, ethane are mixed, obtain unstripped gas,
Wherein, in unstripped gas, acetylene is 1:3.5:1 with hydrogen and methane mol ratio, and in unstripped gas, water vapour content is 2000ppm,
Carbon dioxide is 1000ppm, and carbon monoxide is 500ppm, and ethane is 200ppm, temperature；Unstripped gas is all pressed as 0.45MPa,
Unstripped gas temperature 30 DEG C.Then by unstripped gas supply in the fluid bed being filled with catalyst, and in fluid bed with unstripped gas
Contact portion is graphite material, and wherein, catalyst is prepared from by infusion process, and particle diameter is 20～40 mesh, activity component metal
For palladium, copper and nickel, load capacity is the 0.05wt% of carrier, and catalyst carrier is bead, and reactor operation air speed is 3000h-1,
Reaction temperature is to react at 750 DEG C, obtain containing benzene, ethylene, ethane, butylene, butadiene, vinylacetylene and
The reaction mass of cyclo-octatetraene, then carries out separating treatment to reaction mass, it is hereby achieved that benzene and ethylene.
Embodiment 4
Acetylene, hydrogen, methane, steam and carbon dioxide, carbon monoxide are mixed, obtains unstripped gas, wherein,
In unstripped gas, acetylene is 1:2:4 with hydrogen and methane mol ratio, and in unstripped gas, water vapour content is 1000ppm, titanium dioxide
Carbon is 1000ppm, and carbon monoxide is 500ppm；Unstripped gas is all pressed as 0.95MPa, and unstripped gas temperature is 90 DEG C.Then will
Unstripped gas supplies to the fluid bed being filled with catalyst, and is quartz material with feed gas part in fluid bed, its
In, catalyst is prepared from by infusion process, and particle diameter is 20～40 mesh, and activity component metal is palladium, copper and nickel, and load capacity is
The 0.05wt% of carrier, catalyst carrier is bead, and reactor operation air speed is 10000h-1, reaction temperature is at 450 DEG C
React, obtain containing benzene, ethylene, ethane, butane, butadiene, vinylacetylene, divinylacetylene and ring pungent
The reaction mass of tetraene, then carries out separating treatment to reaction mass, it is hereby achieved that benzene and ethylene.
Comparative example 1
Acetylene, hydrogen, methane, steam are mixed, obtain unstripped gas, wherein, in unstripped gas acetylene and hydrogen and
Methane mol ratio is 1:10:4, and in unstripped gas, water vapour content is 500ppm, temperature 90 DEG C, and unstripped gas is all pressed as 0.95MPa,
Then by unstripped gas supply to be filled with catalyst the most calandria type fixed bed in, wherein, catalyst prepared by infusion process and
Becoming, particle diameter is 20～40 mesh, and activity component metal is palladium, copper and nickel, and load capacity is the 1.5wt% of carrier, catalyst carrier
For glass fiber mesh, reactor operation air speed is 3000h-1, reaction temperature is to react at 450 DEG C, obtain containing benzene,
The reaction mass of ethylene, ethane, butane, butadiene, vinylacetylene, divinylacetylene and cyclo-octatetraene, the most right
Reaction mass carries out separating treatment, it is hereby achieved that benzene and ethylene.
Comparative example 2
Acetylene, hydrogen, methane, steam and carbon dioxide, carbon monoxide are mixed, obtains unstripped gas, wherein,
In unstripped gas, acetylene is 1:6:2 with hydrogen and methane mol ratio, and in unstripped gas, water vapour content is 5000ppm, titanium dioxide
Carbon is 200ppm, and carbon monoxide is 1000ppm, unstripped gas temperature 30 DEG C, and unstripped gas is all pressed as 0.45MPa, then by former
Material gas supplies to the fluid bed without liner being filled with catalyst, and wherein, catalyst is prepared from by infusion process, particle diameter
Being 20～40 mesh, activity component metal is palladium, copper and nickel, and load capacity is the 0.7wt% of carrier, and catalyst carrier is bead,
Reactor operation air speed is 30000h-1, reaction temperature is to react at 750 DEG C, obtains containing benzene, ethylene, ethane, fourth
The reaction mass of alkane, butadiene, vinylacetylene, divinylacetylene and cyclo-octatetraene, is then carried out reaction mass point
From process, it is hereby achieved that benzene and ethylene.
Evaluate:
1, respectively the productivity of conversion of alkyne, the productivity of benzene and ethylene in embodiment 1-4 and comparative example 1-2 is evaluated.
2, HP 6890-5937GC-MS combined instrument is utilized；GC7900 (fid detector, capillary column) and 400MHz
Nuclear magnetic resonance analyser detects each embodiment and the product of comparative example gained, calculating conversion of alkyne, and ethylene and the selectivity of benzene.
Test result is as shown in table 1:
The selectivity contrast of table 1 conversion of alkyne, the selectivity of benzene and ethylene
| Conversion of alkyne (%) | Benzene selective (%) | Ethylene selectivity (%) | |
| Embodiment 1 | 100 | 45.6 | 23.5 |
| Embodiment 2 | 97.9 | 40.0 | 14.9 |
| Embodiment 3 | 100 | 37.1 | 28.9 |
| Embodiment 4 | 98.3 | 39.9 | 29.4 |
| Comparative example 1 | 95.6 | 28.7 | 11.4 |
| Comparative example 2 | 97.2 | 19.2 | 14.3 |
In the description of this specification, reference term " embodiment ", " some embodiments ", " example ", " concrete example ",
Or specific features, structure, material or the feature bag that the description of " some examples " etc. means to combine this embodiment or example describes
It is contained at least one embodiment or the example of the present invention.In this manual, to the schematic representation of above-mentioned term necessarily
It is directed to identical embodiment or example.And, the specific features of description, structure, material or feature can be arbitrary
Individual or multiple embodiment or example combine in an appropriate manner.Additionally, in the case of the most conflicting, the skill of this area
The feature of the different embodiments described in this specification or example and different embodiment or example can be combined by art personnel
And combination.
Although above it has been shown and described that embodiments of the invention, it is to be understood that above-described embodiment is exemplary,
Being not considered as limiting the invention, those of ordinary skill in the art within the scope of the invention can be to above-described embodiment
It is changed, revises, replaces and modification.
Claims (10)
1. an acetylene prepares benzene and the method for coproduction ethylene, it is characterised in that including:
(1) acetylene, hydrogen, methane and steam are mixed, in order to obtain unstripped gas；
(2) supply of described unstripped gas is reacted to the reactor be provided with catalyst；
(3) the reacted material that step (2) obtains is carried out separating treatment, in order to obtain benzene and ethylene.
Method the most according to claim 1, it is characterised in that in described unstripped gas, described acetylene, described hydrogen,
The mol ratio of described methane is 1:(1～3.5): (1～4), the content of described steam is 100～2000ppm, described unstripped gas
Temperature is not higher than 90 degrees Celsius.
Method the most according to claim 1 and 2, it is characterised in that described unstripped gas farther includes other components,
Other components described are at least one in ethane, carbon dioxide and carbon monoxide, and each constituent content is not higher than
1000ppm。
Method the most according to claim 3, it is characterised in that described catalyst for comprising active component and carrier, institute
Stating active component is one or more in group VIII metal, or in group VIII metal and silver, copper, titanium, gallium, molybdenum and indium
One or more combinations formed, wherein, the load capacity of described active component accounts for 0.01wt%～0.1wt% of described carrier.
5. according to the method described in any one of claim 1-4, it is characterised in that described carrier is selected from SiO2、α-Al2O3、
TiO2, at least one in glass fiber mesh and bead.
Method the most according to claim 1, it is characterised in that in step (2), the temperature of described reaction is 400～800
Degree Celsius, pressure is not higher than 1.0MPa.
Method the most according to claim 1, it is characterised in that described reactor is fluid bed, moving bed or shell and tube
Fixed bed, wherein, described fluid bed air speed is 1000～50000ml/ (g cat h), and described moving bed or described shell and tube are fixed
Bed air speed is 500～5000h-1。
8. according to the method according to any one of claim 1-7, it is characterised in that the reaction zone of described reactor is with described
The part of feed gas is non-metallic material, and wherein, described non-metallic material is selected from graphite, enamel, ceramic and quartzy
In at least one.
Method the most according to claim 1, it is characterised in that described reaction mass farther include ethane, butane,
In butylene, butadiene, vinylacetylene, divinylacetylene and cyclo-octatetraene at least one.
10. according to the method according to any one of claim 1-9, it is characterised in that the particle diameter of described catalyst is 20-40
Mesh.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106902889A (en) * | 2017-02-24 | 2017-06-30 | 北京神雾环境能源科技集团股份有限公司 | Benzene catalyst processed and application thereof |
| CN107138100A (en) * | 2017-07-03 | 2017-09-08 | 北京华福工程有限公司 | A kind of apparatus and method that light aromatics is prepared by acetylene |
| CN110673557A (en) * | 2019-09-27 | 2020-01-10 | 南京大学 | Intelligent chemical system based on process condition selection |
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| US5118893A (en) * | 1991-05-24 | 1992-06-02 | Board Of Regents, The University Of Texas System | Zeolite catalyzed conversion of acetylene |
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| US4424401A (en) * | 1980-08-12 | 1984-01-03 | The Broken Hill Proprietary Company Limited | Aromatization of acetylene |
| US5118893A (en) * | 1991-05-24 | 1992-06-02 | Board Of Regents, The University Of Texas System | Zeolite catalyzed conversion of acetylene |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106902889A (en) * | 2017-02-24 | 2017-06-30 | 北京神雾环境能源科技集团股份有限公司 | Benzene catalyst processed and application thereof |
| CN107138100A (en) * | 2017-07-03 | 2017-09-08 | 北京华福工程有限公司 | A kind of apparatus and method that light aromatics is prepared by acetylene |
| CN107138100B (en) * | 2017-07-03 | 2020-05-22 | 北京华福工程有限公司 | Device and method for preparing light aromatic hydrocarbon from acetylene |
| CN110673557A (en) * | 2019-09-27 | 2020-01-10 | 南京大学 | Intelligent chemical system based on process condition selection |
| CN110673557B (en) * | 2019-09-27 | 2021-09-24 | 南京大学 | Intelligent chemical system based on process condition selection |
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