CN110963880A - Ethane oxidation to ethylene process using carbon dioxide as feed gas diluent - Google Patents
Ethane oxidation to ethylene process using carbon dioxide as feed gas diluent Download PDFInfo
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- ethane
- ethylene
- energy consumption
- oxygen
- carbon dioxide
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- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 56
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 239000005977 Ethylene Substances 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 43
- 239000003085 diluting agent Substances 0.000 title claims abstract description 15
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims description 29
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims description 23
- 230000003647 oxidation Effects 0.000 title claims description 12
- 238000007254 oxidation reaction Methods 0.000 title claims description 12
- 239000001569 carbon dioxide Substances 0.000 title claims description 11
- 239000002994 raw material Substances 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 23
- 239000001301 oxygen Substances 0.000 claims description 23
- 229910052760 oxygen Inorganic materials 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 9
- 229910000484 niobium oxide Inorganic materials 0.000 claims description 7
- 229910052714 tellurium Inorganic materials 0.000 claims description 7
- PORWMNRCUJJQNO-UHFFFAOYSA-N tellurium atom Chemical compound [Te] PORWMNRCUJJQNO-UHFFFAOYSA-N 0.000 claims description 7
- WUJISAYEUPRJOG-UHFFFAOYSA-N molybdenum vanadium Chemical group [V].[Mo] WUJISAYEUPRJOG-UHFFFAOYSA-N 0.000 claims description 6
- URLJKFSTXLNXLG-UHFFFAOYSA-N niobium(5+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[O-2].[O-2].[Nb+5].[Nb+5] URLJKFSTXLNXLG-UHFFFAOYSA-N 0.000 claims description 6
- 229910003455 mixed metal oxide Inorganic materials 0.000 claims description 4
- 238000003672 processing method Methods 0.000 claims 1
- 239000012495 reaction gas Substances 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 26
- 238000004230 steam cracking Methods 0.000 abstract description 13
- 238000005516 engineering process Methods 0.000 abstract description 10
- 230000009467 reduction Effects 0.000 abstract description 10
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 abstract description 4
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 34
- 238000006555 catalytic reaction Methods 0.000 description 12
- 239000000463 material Substances 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000005336 cracking Methods 0.000 description 5
- 230000008021 deposition Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000010955 niobium Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- -1 ethylene, propylene, butadiene Chemical class 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- MEFBJEMVZONFCJ-UHFFFAOYSA-N molybdate Chemical compound [O-][Mo]([O-])(=O)=O MEFBJEMVZONFCJ-UHFFFAOYSA-N 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 229910052758 niobium Inorganic materials 0.000 description 1
- GUCVJGMIXFAOAE-UHFFFAOYSA-N niobium atom Chemical compound [Nb] GUCVJGMIXFAOAE-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
Classifications
-
- 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
- C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
- C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- C07C2523/24—Chromium, molybdenum or tungsten
- C07C2523/28—Molybdenum
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention provides a technical method for producing ethylene by oxidative dehydrogenation of ethane by using CO2 as a raw material diluent, belonging to the technical field of petrochemical industry. The invention provides a method for utilizing CO2As raw material gas diluent instead of traditional N2A process for producing ethylene from ethane at low temperature. The method is compared with the traditional ethane steam cracking process (the energy consumption value is 18.5 MJ/kg-C)2H4) Compared with the prior art, the energy consumption can be greatly reduced and is only 11.0MJ/kg-C under better process conditions2H4And a reduction of about 40%. The new ethylene production technology has the characteristics of low raw material unit consumption, particularly low process energy consumption, low investment, less waste and pollutant discharge and the like.
Description
Technical Field
The invention relates to an ethylene production technology of organic chemical industry, and particularly provides a method for producing ethylene by using carbon dioxide (CO)2) The technology of preparing ethylene by oxidative dehydrogenation of ethane as diluent. Compared with the traditional ethane cracking ethylene preparation technology, the invention greatly reduces the unit consumption of raw materials, the energy consumption, the equipment investment and the like, belongs to the technical field of petrochemical industry, and particularly adopts CO2Instead of the usual nitrogen gas (N)2) As a diluent, the energy consumption can be further greatly reduced.
Background
Ethylene is a basic raw material of petrochemical industry, is a prop industry of national economy, and 75 percent of petrochemical products are produced by ethylene at present; ethylene production has become an important indicator of the state petrochemical industry. By 2017, the annual capacity of ethylene in China is 2362 ten thousand tons, the yield is 1822 ten thousand tons, the equivalent consumption is 3900 ten thousand tons, the equivalent self-supporting rate is only 46.7 percent, and a large gap exists. Ethylene is mainly produced industrially through steam thermal cracking reaction including ethane at present, and the process usually requires high-temperature strong endothermic reaction at 800-1100 ℃, so that the process has the following problems: 1. high energy consumption. According to the related literature [ A proceedings of the 8thThe Ethylene Producer Conference AIChE, New York reports that the energy consumption of the process can reach 18.5MJ/kg-C2H4And the process is optimized for many years and is mature, so that the difficulty of further reduction is extremely high. 2. The product composition is complex. The cleavage reaction being a complex radical reactionThe more products produced, on the one hand, will reduce the selectivity of ethylene (ethylene generally not more than 83%), i.e. reduce the utilization rate of raw materials, and on the other hand, will increase the difficulty of separating the products (especially producing low-boiling point H)2And methane). The problems brought about are that the separation equipment is more and the separation energy consumption is high. 3. The carbon deposit needs to be removed periodically. The carbon deposition on the tube wall is caused by high temperature reaction, and the carbon deposition needs to be removed periodically by stopping, so that the production efficiency is influenced. 4. The equipment investment is high. The high-temperature reaction needs an alloy cracking furnace reactor made of special materials, so the equipment investment is high. Therefore, the development of a low-energy-consumption and more environment-friendly ethylene production technical route is an urgent problem related to the development of the ethylene industry.
Undoubtedly, an oxidizing agent (e.g., O) is introduced2Or Air, etc.) to change the ethane cracking reaction from a strong endothermic reaction into a simple exothermic reaction, which becomes one of the ideas of the majority of researchers. The literature [ chem.week, 137(4), 36,1985 ] reports that the energy consumption of the process can be reduced by 20-30%. However, the process thermodynamically favors the deep oxidation product CO2And CO formation, thus, how to improve the selectivity of ethylene becomes the most central technical problem. We have successfully developed a high performance catalyst for the oxidative dehydrogenation of ethylene oxide to ethylene, and the preparation technology of the catalyst is disclosed in patent (ZL 201410198867.2): the conversion rate of ethane is high (60-80%), the selectivity of ethylene is very high (92-96 mol%), and long-time catalyst life experiments prove that the catalyst has very good reaction stability. According to our inventive process (CN201810492035X), N is used2When the catalyst is used as a raw material gas diluent, the energy consumption can be reduced by at least 23 percent compared with the prior ethane steam cracking process.
The process for preparing ethylene by oxidative dehydrogenation of ethane, as an emerging process in development, must have great technical advantages to be possible to completely replace the existing well-established process, namely the process for preparing ethylene by steam cracking of ethane.
Disclosure of Invention
The invention aims to provide a method for utilizing CO2As diluent, replacing traditional nitrogen, ethane produces ethylene at low temperatureThe process method of (1). The method is compared with the traditional ethane steam cracking process (the energy consumption value is 18.5 MJ/kg-C)2H4) Compared with the prior art, the energy consumption can be greatly reduced and is only 11.0MJ/kg-C under better process conditions2H4And a reduction of about 40%.
A process for preparing ethylene by oxidizing ethane features that ethane, oxygen and carbon dioxide are used as raw materials, and the raw materials are catalytically oxidized in the presence of mixed metal oxide catalyst to obtain ethylene.
The carbon dioxide acts as a diluent for the reactant gases ethane and oxygen.
The mixed metal oxide catalyst is a tellurium niobium molybdate catalyst.
In the method, the mole percentage of ethane is 2-60%, the mole percentage of oxygen is 1-30%, and the mole percentage of carbon dioxide is 10-97% respectively.
In the method, the mole percentage of ethane is 10-30%, the mole percentage of oxygen is 5-15%, and the mole percentage of carbon dioxide is 55-85% respectively. The invention adopts CO2In place of N2As a raw material gas diluent, the aim is to further reduce the energy consumption of the new process. CO22Can be liquefied at-56.6 ℃ under lower pressure (0.52 MPa). The invention is based on the use of CO2Special property of easy liquefaction, in the reaction of ethane oxidation to ethylene, replacing N2As a diluent.
The invention provides an ethylene production technology which adopts CO2Is used as raw material gas diluent, and is passed through the process of ethane catalytic oxidation to obtain product whose composition is simple, only contains ethylene, acetic acid, CO and CO2Unreacted ethane and water. Therefore, the product separation is easy, and the energy consumption for separation is low. The invention provides an ethylene production technology which adopts CO2The catalyst is used as a raw material gas diluent, and carbon deposition does not occur on the catalyst in the process of catalytic oxidation of ethane due to the existence of oxygen and water, so that the periodic shutdown treatment is not needed, and the improvement of the production efficiency and the reduction of the operation cost are facilitated.
The invention provides an ethylene production technology which adopts CO2The catalyst is used as a raw material gas diluent, and is a low-temperature process (300-400 ℃) through an ethane catalytic oxidation process, and the requirements on equipment materials in the new process are low according to common knowledge, so that the equipment investment can be reduced.
Detailed Description
The present invention will be further described with reference to the following examples, but the present invention is not limited to these examples.
Example 1
With ethane, oxygen and CO2The preparation method comprises performing catalytic reaction on a molybdenum-vanadium-tellurium-niobium oxide catalyst (the preparation technology of the catalyst is shown in patent ZL201410198867.2) by adopting a fixed bed process, and performing catalytic reaction on ethane, oxygen and CO2The molar ratio of the three materials is 2:1:97, the reaction temperature is 380 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 60% and ethylene selectivity 95%. The energy consumption is 14.5MJ/kg-C2H4A reduction of about 21.6% compared to conventional ethane steam cracking processes.
Example 2
With ethane, oxygen and CO2The raw materials are subjected to catalytic reaction on a molybdenum vanadium tellurium niobium oxide catalyst by adopting a fixed bed process, and ethane, oxygen and CO are subjected to catalytic reaction2The molar ratio of the three materials is 60:30:10, the reaction temperature is 380 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 65% and ethylene selectivity 92%. The energy consumption is 14.2MJ/kg-C2H4A reduction of about 23.2% compared to conventional ethane steam cracking processes.
Example 3
With ethane, oxygen and CO2The raw materials are subjected to catalytic reaction on a molybdenum vanadium tellurium niobium oxide catalyst by adopting a fixed bed process, and ethane, oxygen and CO are subjected to catalytic reaction2The molar ratio of the three materials is 10:5:85, the reaction temperature is 380 ℃, and the total airspeed is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 65% and ethylene selectivity 95%. The energy consumption is 12.5MJ/kg-C2H4A reduction of about 32.4% compared to a conventional ethane steam cracking process.
Example 4
With ethane, oxygen and CO2The raw materials are subjected to catalytic reaction on a molybdenum vanadium tellurium niobium oxide catalyst by adopting a fixed bed process, and ethane, oxygen and CO are subjected to catalytic reaction2The molar ratio of the three materials is 30:15:55, the reaction temperature is 380 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 68% and ethylene selectivity 95%. The energy consumption is 11.1MJ/kg-C2H4A reduction of about 40.0% compared to conventional ethane steam cracking processes.
Example 5
With ethane, oxygen and CO2The raw materials are subjected to catalytic reaction on a molybdenum vanadium tellurium niobium oxide catalyst by adopting a fixed bed process, and ethane, oxygen and CO are subjected to catalytic reaction2The molar ratio of the three materials is 20:10:70, the reaction temperature is 380 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 69%, ethylene selectivity 95%. The energy consumption is 11.5MJ/kg-C2H4A reduction of about 37.8% compared to conventional ethane steam cracking processes.
Example 6
With ethane, oxygen and CO2The raw materials are subjected to catalytic reaction on a molybdenum vanadium tellurium niobium oxide catalyst by adopting a fixed bed process, ethane, oxygen and H2The molar ratio of the three materials such as O and the like is 30:15:55, the reaction temperature is 370 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. Ethane conversion 56%, product selectivities were as follows: ethylene selectivity 96%, acetic acid selectivity 0.5%, CO selectivity 2.4%, CO2The selectivity was 1.1%. No other carbonaceous products were detected by chromatography in the experiment. The total energy consumption in the process is 11.5MJ/kg-C2H4A reduction of about 32.4% compared to a conventional ethane steam cracking process. The product separation energy consumption of the process is 4.6MJ/kg-C2H4And the energy consumption for separating products in the traditional ethane steam cracking process is 9.0MJ/kg-C2H4The separation energy consumption is remarkably reduced.
Example 7
With ethane, oxygen and CO2As raw material, on Mo-V-Te-Nb oxide catalystFixed bed process for catalytic reaction of ethane, oxygen and H2The molar ratio of the three materials such as O and the like is 30:15:55, the reaction temperature is 400 ℃, and the total space velocity is 7500h-1The reaction pressure is 0.85 MPa. The reaction was run for 3000h, with the following catalyst properties: the ethane conversion was about 79% and the ethylene selectivity was about 93%, which remained essentially unchanged. Particularly, the carbon balance is kept between 98% and 102%, the catalyst is subjected to element analysis after the reaction is finished, and the existence of carbon elements is not detected in the catalyst, so that the phenomenon of carbon deposition does not occur in the whole reaction process.
Comparative example 1
The "current development and thinking of ethylene production by ethane cracking at home and abroad" published by huangge province and others in the research paper of "modern chemical engineering" volume 38, phase 10, shows that the products of the ethane cracking process include more than ten products such as methane, ethylene, propylene, butadiene, butane, butylene, benzene, toluene, C8 aromatic hydrocarbon, raffinate oil, heavy oil and hydrogen.
Comparative example 2
Li Jianhua et al published in the research paper "comprehensive energy consumption analysis research progress of ethylene production process by steam cracking" of energy saving, No. 10 (2008), indicated that the typical value of comprehensive energy consumption of a steam cracking technology using ethane as a raw material is 17-21 GJ/t ethylene (i.e. 17-21 MJ/kg ethylene).
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| Application Number | Priority Date | Filing Date | Title |
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| CN2018111419888 | 2018-09-28 | ||
| CN201811141988 | 2018-09-28 |
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| CN110963880A true CN110963880A (en) | 2020-04-07 |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1076925A (en) * | 1990-10-05 | 1993-10-06 | 罗纳·布朗克化学公司 | The controlled oxidation of ethane is to produce the method for ethene and acetate mixture |
| CN1441767A (en) * | 2000-05-19 | 2003-09-10 | 国际人造丝公司 | Method for selective production of acetic acid by catalystic oxidation of ethane and/or ethylene |
| CN103965002A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Oxidative dehydrogenation method used for low-carbon-number hydrocarbons |
| CN105080575A (en) * | 2014-05-12 | 2015-11-25 | 中国科学院大连化学物理研究所 | Molybdenum vanadium tellurium niobium oxygen catalyst for preparing ethene from ethane and preparation method and application |
| US20160326070A1 (en) * | 2014-01-30 | 2016-11-10 | Linde Aktiengesellschaft | Diluting alkane oxydehydrogenation reactants with carbon dioxide |
| CN111032601A (en) * | 2017-08-16 | 2020-04-17 | 国际壳牌研究有限公司 | Ethane Oxidative Dehydrogenation |
| CN111032600A (en) * | 2017-08-16 | 2020-04-17 | 国际壳牌研究有限公司 | Oxidative dehydrogenation of ethane |
-
2019
- 2019-02-15 CN CN201910117371.0A patent/CN110963880A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1076925A (en) * | 1990-10-05 | 1993-10-06 | 罗纳·布朗克化学公司 | The controlled oxidation of ethane is to produce the method for ethene and acetate mixture |
| CN1441767A (en) * | 2000-05-19 | 2003-09-10 | 国际人造丝公司 | Method for selective production of acetic acid by catalystic oxidation of ethane and/or ethylene |
| CN101041135A (en) * | 2000-05-19 | 2007-09-26 | 国际人造丝公司 | Method for selectively preparing acetic acid by catalytic oxidation of ethane and/or ethylene |
| CN103965002A (en) * | 2013-01-30 | 2014-08-06 | 中国石油化工股份有限公司 | Oxidative dehydrogenation method used for low-carbon-number hydrocarbons |
| US20160326070A1 (en) * | 2014-01-30 | 2016-11-10 | Linde Aktiengesellschaft | Diluting alkane oxydehydrogenation reactants with carbon dioxide |
| CN105080575A (en) * | 2014-05-12 | 2015-11-25 | 中国科学院大连化学物理研究所 | Molybdenum vanadium tellurium niobium oxygen catalyst for preparing ethene from ethane and preparation method and application |
| CN111032601A (en) * | 2017-08-16 | 2020-04-17 | 国际壳牌研究有限公司 | Ethane Oxidative Dehydrogenation |
| CN111032600A (en) * | 2017-08-16 | 2020-04-17 | 国际壳牌研究有限公司 | Oxidative dehydrogenation of ethane |
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Application publication date: 20200407 |