CN110041156A - A kind of integrated technique of methane direct conversion ethylene - Google Patents
A kind of integrated technique of methane direct conversion ethylene Download PDFInfo
- Publication number
- CN110041156A CN110041156A CN201910464446.2A CN201910464446A CN110041156A CN 110041156 A CN110041156 A CN 110041156A CN 201910464446 A CN201910464446 A CN 201910464446A CN 110041156 A CN110041156 A CN 110041156A
- Authority
- CN
- China
- Prior art keywords
- methane
- ethylene
- cavity
- direct conversion
- ethane
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
- C07C2/82—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling
- C07C2/84—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
-
- 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
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
-
- 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
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention relates to methane transformation technology fields, more particularly to a kind of integrated technique of methane direct conversion ethylene.A kind of integrated technique by methane direct conversion ethylene, carry out oxidative coupling of methane and alkane cracking reaction simultaneously in the different cavities of coupled reactor, oxidative coupling of methane releasing heat is carried out under the first catalyst action containing methane, oxygen feed gas into the first cavity, heat passes to the second cavity by interlayer wall, into the ethane and C in the second cavity2+Mixture carries out alkane cracking reactive absorption heat under the second catalyst action, and coupled reactor is the collet filling bed type that tube side and shell side are constituted or coupled reactor is tubulation shell journey heat exchange type.
Description
Technical field
The present invention relates to methane transformation technology fields, more particularly to a kind of integrated work of methane direct conversion ethylene
Skill.
Background technique
Ethylene is a kind of important large petrochemicals, even more a kind of large industrial chemicals.Currently, production ethylene
Route includes petroleum base route and coal base route, and wherein petroleum base route is mainly hydrocarbon cracking method, i.e., is with ethane and propane
Cracking stock produces ethylene through tubular type thermal cracking.However, being only that cracking is former with second, propane with the continuous promotion of alkene demand
Material starts to develop to heaviness far from meeting the needs of market is to alkene, cracking stock.In recent years, the Chinese Academy of Sciences's bigization institute and it is upper
The coal base ethylene route MTO technology that extra large petrochemical industry project company develops respectively, has become novel ethylene production.MTO
Technology, i.e. coal can cross this method for coal gasification, gas purification, methanol-fueled CLC, refining methanol, methanol alkene through methanol-to-olefins
Hydrocarbon, separation of olefins and etc., obtain ethylene, propylene product.Energy of this method in China's " oil starvation, few gas, coal relative abundance "
Under source structure background, the alternative of a kind of ethylene, production of propylene is provided, but this method there are synthetic routes long, equipment
Invest excessive disadvantage.For this purpose, this patent provides a kind of technique of methane direct conversion ethylene, it is intended to it is aoxidized by a step,
It is ethylene by methane direct conversion.This technique has the advantages that synthetic route is short, equipment investment is small.Meanwhile in the world,
It is exploited as the reserves of the natural gases such as shale gas, coal bed gas are clear with positive, technique will provide raw material abundant thus, guarantee
The Technical Economy of this technique.
Summary of the invention
The technical problems to be solved by the present invention are: how to provide a kind of integrated technique of methane direct conversion ethylene.
The technical scheme adopted by the invention is that: a kind of integrated technique by methane direct conversion ethylene, it is anti-in coupling
Oxidative coupling of methane and alkane cracking reaction are answered in the different cavities of device while being carried out, contains first into the first cavity
Alkane, oxygen feed gas carry out oxidative coupling of methane under the first catalyst action and release heat, and heat is passed by interlayer wall
The second cavity is passed, into the ethane and C in the second cavity2+It is anti-that mixture carries out alkane cracking under the second catalyst action
Heat should be absorbed, coupled reactor is the collet filling bed type that tube side and shell side are constituted or coupled reactor is tubulation shell journey
Heat exchange type.
The product generated in the first cavity by oxidative coupling of methane, it is de- by dehydration-into separative unit
Carbon-drying, demethanation and de- ethylene process, finally obtain ethylene, and the unreacted methane gas obtained during demethanation is made
Enter the first container for unstripped gas to recycle, the ethane and C2+ mixture obtained from de- ethylene process enters second container ginseng
It is reacted with alkane cracking.
Into, containing in methane, oxygen feed gas, the volume ratio of methane and oxygen is 2-20, and temperature is in the first cavity
500 ~ 800 DEG C, pressure is 0.1 MPa -1 MPa.
The optional published all methane oxidative coupling catalysts of catalyst of the present invention and alkane dehydrogenating catalyst, it is especially suitable
For patent CN201811460300.2, methane oxidation disclosed in CN201811459030.3, CN201811459097.7 is even
Join alkane dehydrogenating catalyst disclosed in catalyst and patent CN201610134338.5, CN201610003116.
First cavity reaction raw materials include: pure methane gas or high methane gas, pure oxygen or oxygen-containing gas.Unstripped gas can source
In natural gas, casing-head gas, refinery gas, shale gas, coal bed gas and device in Gas.Reactor feed gas charge order is: 1) methane or
Methane-rich gas and oxygen or oxygen-containing gas are imported from coupled reactor the first cavity front end jointly, with methane-oxidizing and-coupling
Agent contact.It can be pre-mixed between unstripped gas, reactor can also be introduced directly into.2) pass through methane oxidative coupling catalyst bed
The reaction product gas of layer, into separative unit, carries out being dehydrated-decarburization-drying, demethanation and de- ethylene mistake through heat recovery
Journey finally obtains ethylene, and the unreacted methane gas obtained from demethanation unit is recycled as unstripped gas, from de- ethylene list
The ethane and C2+ mixture that member obtains pass through the second cavity of reactor alkane dehydrogenating catalyst bed.3) it is urged by dehydrating alkanes
Reaction product gaseous mixture after agent bed enters separative unit.4) two are loaded respectively in two cavities of same coupled reactor
Class catalyst can fill out cavity dress oxidative coupling catalyst first and realize oxidative coupling of methane, fill alkane in the second cavity
Hydrocarbon dehydrogenation realizes dehydrating alkanes reaction；Conversely, alkane dehydrogenating catalyst can also be filled in the second cavity, the first cavity is loaded
Methane oxidative coupling catalyst, since oxidative coupling of methane, dehydrating alkanes react respectively exothermic reaction, the endothermic reaction,
Whole be thermally integrated can be achieved.
Coupled reactor go into operation heating method can using electric heating, diamond heating, can also using other routinely plus
The combination of hot mode or several heating methods.After reacting and reaching certain temperature, coupled reactor heat exchange reaches autothermal equilibrium,
It shows preferably to be thermally integrated advantage.
The present invention due to using two kinds react put, heat absorptivity, by two reaction be fully thermally integrated in same reactor,
Reactor autothermal equilibrium is realized, the reasonable utilization of energy is realized, improves the economy of technique.
Detailed description of the invention
Fig. 1 is integrated artistic flow diagram proposed by the present invention；
The collet filling bed type coupled reactor that Fig. 2 tube side and shell side are constituted；
Fig. 3 is tubulation shell journey heat exchange type coupled reactor；
Wherein, the 1, first cavity entrance, the 2, first chamber outlet, the 3, second cavity entrance, the 4, second chamber outlet, 5, first holds
Chamber, the 6, second cavity.
Specific embodiment
The following further describes the present invention with reference to the drawings.
Example 1
By OCM catalyst disclosed in 5mL Chinese patent CN201811460300.2 and 20mL Chinese patent CN201610003116
Disclosed ethane dehydrogenation catalyst is respectively implanted in the first cavity (tube side) 5 and the second cavity (shell side) 6 of reactor (Fig. 2).
Operating procedure is as follows:
(1) in nitrogen atmosphere, OCM catalyst is heated to 500 DEG C.It is then shut off nitrogen, and is fed by tube-side inlet 1
240mL/min methane, 60mL/min oxygen, at 600 DEG C of temperature, pressure 0.1MPa, finally in the logistics of 2 acquisition of tube side outlet
Middle ethylene concentration is 8.2%, yield of ethene 16.3%.
(2) 120mL/min ethane is fed by shell side inlet 3, uneven shell-side temperature maintains 550 DEG C after stablizing, and pressure is
0.1MPa, shell-side outlet 4 obtain logistics in ethylene concentration be 31.2%, ethane conversion 48%.
(3) after heat matching balance, tube side temperature maintains 596 DEG C, and pressure maintains 0.1MPa, and tube side outlet 2 obtains
Ethylene concentration is 7.9% in the logistics obtained, yield of ethene 16.1%；Uneven shell-side temperature maintains 557 DEG C, and pressure maintains
0.1MPa, shell side produce 4 obtain logistics in ethylene concentration be 31.5%, ethane conversion 49%.
Tube side OCM exothermic reaction can be filled with the endothermic reaction of shell side ethane dehydrogenation to ethene it can be seen from above-mentioned experiment
Divide and be coupled, while carrying out OCM reaction, converts ethylene for the ethane in by-product, realize ethylene volume increase.In addition,
Shell side more greatly increasing output of ethylene can be entered with additional ethane.
Example 2
By OCM catalyst disclosed in 5mL Chinese patent CN201811460300.2 and 20mL Chinese patent
Ethane dehydrogenation catalyst disclosed in CN201610134338.5 is respectively implanted the first cavity (tube side) 5 and the second cavity of reactor
In (shell side) 6 (Fig. 2).Operating procedure is as follows:
(1) in nitrogen atmosphere, OCM catalyst is heated to 700 DEG C.It is then shut off nitrogen, and is fed by tube-side inlet 1
240mL/min methane, 60mL/min oxygen, at 750 DEG C of temperature, pressure 0.1MPa, finally in the logistics of 2 acquisition of tube side outlet
Middle ethylene concentration is 12.7%, yield of ethene 24.1%.
(2) 150mL/min ethane is fed by shell side inlet 3, uneven shell-side temperature maintains 650 DEG C after stablizing, and pressure is
0.1MPa, shell-side outlet 4 obtain logistics in ethylene concentration be 31.6%, ethane conversion 53%.
(3) after heat matching balance, tube side temperature maintains 743 DEG C, and pressure maintains 0.1MPa, and tube side outlet 2 obtains
Ethylene concentration is 12.3% in the logistics obtained, yield of ethene 23.8%；Uneven shell-side temperature maintains 687 DEG C, and pressure maintains
0.1MPa, shell side produce 4 obtain logistics in ethylene concentration be 31.9%, ethane conversion 54%.
Tube side OCM exothermic reaction can be filled with the endothermic reaction of shell side ethane dehydrogenation to ethene it can be seen from above-mentioned experiment
Divide and be coupled, while carrying out OCM reaction, converts ethylene for the ethane in by-product, realize ethylene volume increase.In addition,
Shell side more greatly increasing output of ethylene can be entered with additional ethane.
Example 3
By OCM catalyst disclosed in 5mL Chinese patent CN201811459030.3 and 20mL Chinese patent
Ethane dehydrogenation catalyst disclosed in CN201610134338.5 is respectively implanted the first cavity (tube side) 5 and the second cavity of reactor
In (shell side) 6 (Fig. 2).Operating procedure is as follows:
(1) in nitrogen atmosphere, OCM catalyst is heated to 675 DEG C.It is then shut off nitrogen, and is fed by tube-side inlet 1
240mL/min methane, 120mL/min oxygen, at 675 DEG C of temperature, pressure 0.2MPa, finally in the object of 2 acquisition of tube side outlet
Ethylene concentration is 11.8% in stream, yield of ethene 22.1%.
(2) 160mL/min ethane is fed by shell side inlet 3, uneven shell-side temperature maintains 600 DEG C after stablizing, and pressure is
0.1MPa, shell-side outlet 4 obtain logistics in ethylene concentration be 32.7%, ethane conversion 51%.
(3) after heat matching balance, tube side temperature maintains 671 DEG C, and pressure maintains 0.2MPa, and tube side outlet 2 obtains
Ethylene concentration is 11.3% in the logistics obtained, yield of ethene 21.8%；Uneven shell-side temperature maintains 625 DEG C, and pressure maintains
0.1MPa, shell side produce 4 obtain logistics in ethylene concentration be 33.1%, ethane conversion 52%.
Tube side OCM exothermic reaction can be filled with the endothermic reaction of shell side ethane dehydrogenation to ethene it can be seen from above-mentioned experiment
Divide and be coupled, while carrying out OCM reaction, converts ethylene for the ethane in by-product, realize ethylene volume increase.In addition,
Shell side more greatly increasing output of ethylene can be entered with additional ethane.
Example 4
By OCM catalyst disclosed in 5mL Chinese patent CN201811459030.3 and 20mL Chinese patent
Ethane dehydrogenation catalyst disclosed in CN201610134338.5 is respectively implanted the first cavity (tube side) 5 and the second cavity of reactor
In (shell side) 6 (Fig. 2).Operating procedure is as follows:
(1) in nitrogen atmosphere, OCM catalyst is heated to 750 DEG C.It is then shut off nitrogen, and is fed by tube-side inlet 1
240mL/min methane, 90mL/min oxygen, at 750 DEG C of temperature, pressure 0.5MPa, finally in the logistics of 2 acquisition of tube side outlet
Middle ethylene concentration is 13.3%, yield of ethene 24.6%.
(2) 170mL/min ethane is fed by shell side inlet 3, uneven shell-side temperature maintains 700 DEG C after stablizing, and pressure is
0.1MPa, shell-side outlet 4 obtain logistics in ethylene concentration be 35.7%, ethane conversion 58%.
(3) after heat matching balance, tube side temperature maintains 742 DEG C, and pressure maintains 0.5MPa, and tube side outlet 2 obtains
Ethylene concentration is 12.9% in the logistics obtained, yield of ethene 24.1%；Uneven shell-side temperature maintains 698 DEG C, and pressure maintains
0.1MPa, shell side produce 4 obtain logistics in ethylene concentration be 36.2%, ethane conversion 59%.
Tube side OCM exothermic reaction can be filled with the endothermic reaction of shell side ethane dehydrogenation to ethene it can be seen from above-mentioned experiment
Divide and be coupled, while carrying out OCM reaction, converts ethylene for the ethane in by-product, realize ethylene volume increase.In addition,
Shell side more greatly increasing output of ethylene can be entered with additional ethane.
Example 5
By OCM catalyst disclosed in 5mL Chinese patent CN201811459097.7 and 20mL Chinese patent
Ethane dehydrogenation catalyst disclosed in CN201610134338.5 is respectively implanted the first cavity (tube side) 5 and the second cavity of reactor
In (shell side) 6.Operating procedure is as follows:
(1) in nitrogen atmosphere, OCM catalyst is heated to 800 DEG C.It is then shut off nitrogen, and is fed by shell side inlet 3
1200mL/min methane, 60mL/min oxygen, at 800 DEG C of temperature, pressure 1MPa, finally in the logistics of the acquisition of shell-side outlet 4
Middle ethylene concentration is 5.1%, yield of ethene 21.5%.
(2) 150mL/min ethane is fed by tube-side inlet 1, uneven shell-side temperature maintains 750 DEG C after stablizing, and pressure is
0.1MPa, it is 37.6% that tube side, which exports ethylene concentration in the logistics that 2 obtain, ethane conversion 63%.
(3) after heat matching balance, uneven shell-side temperature maintains 791 DEG C, and pressure maintains 1MPa, and shell-side outlet 4 obtains
Logistics in ethylene concentration be 5%, yield of ethene 21.3%；Tube side temperature maintains 754 DEG C, and pressure maintains 0.1MPa, pipe
Ethylene concentration is 38.1 %, ethane conversion 64% in the logistics that journey outlet 2 obtains.
Shell side OCM exothermic reaction can be filled with the endothermic reaction of tube side ethane dehydrogenation to ethene it can be seen from above-mentioned experiment
Divide and be coupled, while carrying out OCM reaction, converts ethylene for the ethane in by-product, realize ethylene volume increase.In addition,
Tube side more greatly increasing output of ethylene can be entered with additional ethane.
Claims (5)
1. a kind of integrated technique of methane direct conversion ethylene, it is characterised in that: same in the different cavities of coupled reactor
Shi Jinhang oxidative coupling of methane and alkane cracking reaction contain methane, oxygen feed gas first into the first cavity
Oxidative coupling of methane is carried out under catalyst action and releases heat, and heat passes to the second cavity by interlayer wall, into the
Ethane and C in two cavities2+Mixture carries out alkane cracking reactive absorption heat, coupled reactor under the second catalyst action
The collet filling bed type or coupled reactor constituted for tube side and shell side is tubulation shell journey heat exchange type.
2. a kind of integrated technique of methane direct conversion ethylene according to claim 1, it is characterised in that: hold first
The product generated in chamber by oxidative coupling of methane, into separative unit, by dehydration-decarburization-drying, demethanation and
De- ethylene process, finally obtains ethylene, and the unreacted methane gas obtained during demethanation enters first as unstripped gas
Container recycles, and the ethane and C2+ mixture obtained from de- ethylene process enters second container and participates in alkane cracking reaction.
3. a kind of integrated technique of methane direct conversion ethylene according to claim 1, it is characterised in that: coupling reaction
The device heating method that goes into operation can also use other conventional heating modes or several heating using electric heating, diamond heating
The combination of mode.
4. a kind of integrated technique of methane direct conversion ethylene according to claim 1, it is characterised in that: enter first
In cavity containing methane, in oxygen feed gas, the volume ratio of methane and oxygen is 2-20, and temperature is 500 ~ 800 DEG C, and pressure is
0.1 MPa -1 MPa。
5. a kind of integrated technique of methane direct conversion ethylene according to claim 1, it is characterised in that: the first catalysis
Agent is methane oxidative coupling catalyst, and the second catalyst is alkane dehydrogenating catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910464446.2A CN110041156A (en) | 2019-05-30 | 2019-05-30 | A kind of integrated technique of methane direct conversion ethylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910464446.2A CN110041156A (en) | 2019-05-30 | 2019-05-30 | A kind of integrated technique of methane direct conversion ethylene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110041156A true CN110041156A (en) | 2019-07-23 |
Family
ID=67284216
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910464446.2A Pending CN110041156A (en) | 2019-05-30 | 2019-05-30 | A kind of integrated technique of methane direct conversion ethylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110041156A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020073853A1 (en) * | 2018-10-08 | 2020-04-16 | 中国石油化工股份有限公司 | Method and system for separating light hydrocarbons |
| CN111450779A (en) * | 2020-04-17 | 2020-07-28 | 安庆泽远化工有限公司 | Reaction device and process for preparing ethylene by oxidative coupling of methane |
| CN113800994A (en) * | 2020-06-17 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
| CN113800995A (en) * | 2020-06-17 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for coupling propane catalytic dehydrogenation reaction and methane oxidative coupling reaction |
| CN113816820A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method for preparing ethylene through methane oxidative coupling reaction |
| CN113816819A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
| CN113816822A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method and system for coupling propane catalytic dehydrogenation reaction and methane oxidative coupling reaction |
| CN113816819B (en) * | 2020-06-18 | 2024-07-02 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN88101761A (en) * | 1987-03-30 | 1988-11-16 | 大西洋里奇费尔德公司 | Methane conversion is become the method and apparatus of the hydrocarbon product of higher |
| WO1993013039A1 (en) * | 1991-12-31 | 1993-07-08 | Amoco Corporation | An olefins process which combines hydrocarbon cracking with methane coupling |
| US5599510A (en) * | 1991-12-31 | 1997-02-04 | Amoco Corporation | Catalytic wall reactors and use of catalytic wall reactors for methane coupling and hydrocarbon cracking reactions |
| WO2013148610A1 (en) * | 2012-03-26 | 2013-10-03 | Sundrop Fuels, Inc. | Various methods and apparatuses for internally heated radiant tubes in a chemical reactor |
| US20140194663A1 (en) * | 2009-03-31 | 2014-07-10 | Fina Technology, Inc. | Oxidative Coupling of Hydrocarbons as Heat Source |
| CN208661079U (en) * | 2018-06-20 | 2019-03-29 | 中国石化工程建设有限公司 | The reactor of thermal coupling catalysis processing hydro carbons |
| CN109678636A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas |
-
2019
- 2019-05-30 CN CN201910464446.2A patent/CN110041156A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN88101761A (en) * | 1987-03-30 | 1988-11-16 | 大西洋里奇费尔德公司 | Methane conversion is become the method and apparatus of the hydrocarbon product of higher |
| WO1993013039A1 (en) * | 1991-12-31 | 1993-07-08 | Amoco Corporation | An olefins process which combines hydrocarbon cracking with methane coupling |
| US5599510A (en) * | 1991-12-31 | 1997-02-04 | Amoco Corporation | Catalytic wall reactors and use of catalytic wall reactors for methane coupling and hydrocarbon cracking reactions |
| US20140194663A1 (en) * | 2009-03-31 | 2014-07-10 | Fina Technology, Inc. | Oxidative Coupling of Hydrocarbons as Heat Source |
| WO2013148610A1 (en) * | 2012-03-26 | 2013-10-03 | Sundrop Fuels, Inc. | Various methods and apparatuses for internally heated radiant tubes in a chemical reactor |
| CN109678636A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas |
| CN208661079U (en) * | 2018-06-20 | 2019-03-29 | 中国石化工程建设有限公司 | The reactor of thermal coupling catalysis processing hydro carbons |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020073853A1 (en) * | 2018-10-08 | 2020-04-16 | 中国石油化工股份有限公司 | Method and system for separating light hydrocarbons |
| US11649406B2 (en) | 2018-10-08 | 2023-05-16 | China Petroleum & Chemical Corporation | Method and system for separating light hydrocarbons |
| CN111450779A (en) * | 2020-04-17 | 2020-07-28 | 安庆泽远化工有限公司 | Reaction device and process for preparing ethylene by oxidative coupling of methane |
| CN111450779B (en) * | 2020-04-17 | 2022-06-28 | 湖北圣灵科技有限公司 | Reaction device and process for preparing ethylene by oxidative coupling of methane |
| CN113800994A (en) * | 2020-06-17 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
| CN113800995A (en) * | 2020-06-17 | 2021-12-17 | 中国石油化工股份有限公司 | Method and system for coupling propane catalytic dehydrogenation reaction and methane oxidative coupling reaction |
| CN113816820A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method for preparing ethylene through methane oxidative coupling reaction |
| CN113816819A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
| CN113816822A (en) * | 2020-06-18 | 2021-12-21 | 中国石油化工股份有限公司 | Method and system for coupling propane catalytic dehydrogenation reaction and methane oxidative coupling reaction |
| CN113816819B (en) * | 2020-06-18 | 2024-07-02 | 中国石油化工股份有限公司 | Method and system for preparing ethylene by coupling methane oxidative coupling reaction and ethane catalytic dehydrogenation reaction |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110041156A (en) | A kind of integrated technique of methane direct conversion ethylene | |
| CN105517978B (en) | The method that methane is changed into ethene | |
| US20120065412A1 (en) | System and process for producing higher-value hydrocarbons from methane | |
| US8884089B2 (en) | Process for producing olefins | |
| CN105541530B (en) | A kind of method that biological methane photo catalytic activation prepares high-carbon hydrocarbon | |
| CN110386853A (en) | A kind of coupling technique of Catalyst for Oxidative Coupling of Methane and methane dry reforming preparing synthetic gas | |
| CN101130469B (en) | Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol | |
| CN103071528A (en) | Core-shell structure catalyst and method for preparing low-carbon olefin by using synthetic gas one-step method | |
| EP2499122B1 (en) | Process for producing ethylene oxide | |
| KR102054837B1 (en) | Radial flow catalytic reactor for exothermic reaction | |
| AU2011244368B2 (en) | Process for producing aromatic hydrocarbons and ethylene | |
| CN109689601A (en) | The method of ethylene is prepared in the propylene preparation process reacted using dehydrogenating propane | |
| CN104098419B (en) | Coal, natural gas combination preparing light olefins from methanol system and method | |
| CN102639676A (en) | Process for producing olefins | |
| CN113574009A (en) | Process for the production of methanol from synthesis gas produced by catalytic partial oxidation combined with cracking | |
| CN107428710A (en) | The system and method relevant with production oxirane, ethylene glycol and/or monoethanolamine | |
| US10821432B2 (en) | Olefin production method comprising reduction pretreatment | |
| CN216513608U (en) | Device for increasing ethylene yield by combining methanol-to-olefin process | |
| EP4082996A1 (en) | Non-catalytic oxidative coupling of methane | |
| CN114656316A (en) | System and method for preparing olefin through oxidative coupling of methane and application of system and method | |
| CN106986736A (en) | A kind of hydrocarbon production technique and hydrocarbon production device | |
| CN117339487A (en) | Reaction device and method for efficiently converting synthesis gas | |
| EA043578B1 (en) | METHOD FOR PRODUCING METHANOL FROM SYNTHESIS GAS PRODUCED BY CATALYTIC PARTIAL OXIDATION INTEGRATED WITH CRACKING | |
| Aimin et al. | An Innovative Approach for Ethylene Production from Natural Gas | |
| EP2847146B1 (en) | Method of making oxygenates from a non-catalytic chemical reaction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190723 |