CN102659500B - Method for producing ethylene and ethane and catalytic reactor - Google Patents
Method for producing ethylene and ethane and catalytic reactor Download PDFInfo
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- CN102659500B CN102659500B CN201210152674.4A CN201210152674A CN102659500B CN 102659500 B CN102659500 B CN 102659500B CN 201210152674 A CN201210152674 A CN 201210152674A CN 102659500 B CN102659500 B CN 102659500B
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Abstract
The invention relates to a method for producing ethylene and ethane and a catalytic reactor, belonging to the technical field of lower hydrocarbon. The method comprises the following steps of: carrying out first methane catalytic conversion reaction on a methane-rich feed gas and an oxidizing gas by using a first section of granular catalytic agent, carrying out second methane catalytic conversion reaction on the gas mixture entering a second integrated type catalytic agent reaction section after supplementing the oxidizing gas in a reaction gas mixture, and finally collecting a reaction product. A premixing chamber which is provided with a feed gas inlet and an oxidizing gas inlet is arranged at the top of the catalytic reactor; a first reactor in which a granular catalytic agent is placed is communicated with the lower end of the premixing chamber; an oxidizing gas replenisher is communicated with the first reactor; a second reactor in which an integral catalytic agent is placed is communicated with the oxidizing gas replenisher; and a product outlet is arranged at the lower end of the second reactor. The catalytic reactor has the advantages that the single-pass methane conversion rate of the methane catalytic conversion reaction is increased, the technological process is short, the operation is stable, and the equipment investment is few.
Description
Technical field
The present invention relates to a kind of ethene, ethane preparation method and realize the catalyticreactor of aforesaid method, belong to lower carbon number hydrocarbons technical field.
Background technology
Be rich in the coal-seam gas of methane, Sweet natural gas, biogas is important resource, except directly as except fuel, through being catalytically conveted to the basic chemical industry such as ethene, ethane raw material, greatly can improving their value added, reducing the consumption of oil simultaneously.Catalysis conversion method can divide indirect method and direct method.
Indirect method first the feed gas catalytic being rich in methane is converted into synthetic gas (mainly CO and H
2), then synthetic gas is made the raw materials such as methyl alcohol, dme, lower carbon number hydrocarbons, finally pass through the low-carbon alkenes such as the method preparing ethylene of catalyzed conversion again.Its subject matter is that technical process is oversize, energy consumption is high, production efficiency is low.
Direct method is exactly under the effect of catalyzer, and will be rich in unstripped gas and the oxidizing gas such as oxygen or the air generation catalyzed reaction of methane, a step is catalytically conveted to the lower carbon number hydrocarbons such as ethene, ethane.The method technical process is simple, easy to operate, has important industrial prospect.
Summary of the invention
The object of the present invention is to provide a kind of be ethene by the unstripped gas direct catalytic conversion being rich in methane, the method for ethane and realize the catalyticreactor of aforesaid method.
For achieving the above object, provided by the invention is ethene by the unstripped gas direct catalytic conversion being rich in methane, the method of ethane, it is the unstripped gas being rich in methane, under the effect of catalyzer, react with oxidizing gas, direct catalytic conversion generates ethene, ethane, it is characterized in that, comprise two section of two class catalyst process, first paragraph is pellet type catalyst, second segment is integral catalyzer two class catalyst process, specifically comprise the following steps: the unstripped gas and the oxidizing gas that are rich in methane during reaction carry out after first time methyl hydride catalyzed conversion reaction through first paragraph pellet type catalyst, in reaction mixture gas, delivery of supplemental oxygen voltinism gas enters second segment integral catalyzer conversion zone again and carries out the methyl hydride catalyzed conversion reaction of second time, last collecting reaction product.
The above-mentioned unstripped gas being rich in methane is that one or more in coal-seam gas, Sweet natural gas, biogas are for unstripped gas; Oxidizing gas is oxygen or air.
Catalyzed reaction of the present invention is preferably carried out under 0.1 ~ 1.5MPa pressure condition, and unstripped gas and oxidizing gas are with 1.0 x 10
2~ 5.0 x 10
6h
-1gas space velocity by catalyzer, the temperature of reaction of first paragraph and second segment catalyst section is all between 700 DEG C ~ 900 DEG C.
In aforesaid method, be rich in the unstripped gass such as the coal-seam gas of methane, Sweet natural gas, biogas, ideal methane volumetric content is more than 90%; What oxidizing gas was ideal is oxygen; During reaction, be 2 ~ 4: 1 by the molar ratio of the methane in the unstripped gas of first paragraph pellet type catalyst and the oxygen in oxidizing gas, ideal is 3: 1; After the first time methyl hydride catalyzed conversion reaction of first paragraph pellet type catalyst, the oxidizing gas supplemented in reaction mixture gas is oxygen or air, ideal is oxygen, and the oxidizing gas amount of supplementing be by the molar ratio of the methane in first paragraph unstripped gas and the oxygen supplemented for (2 ~ 4): (0.01 ~ 0.30) introduces, and ideal is 3: 0.15.The particulate catalyst material of first paragraph is conventional existing Catalyst for Oxidative Coupling of Methane, the catalyzer of ethane, and its structure is granular, and particle diameter is at 2 ~ 10mm; The integral catalyzer material of second segment is conventional existing Catalyst for Oxidative Coupling of Methane, ethane catalyzer, and its structure is the integral catalyzer with pore passage structure.
The unstripped gas direct catalytic conversion being rich in methane of the present invention is the catalyzer of ethene, ethane, and the two sections of bed catalysts combined by certain way by the pellet type catalyst of first paragraph and the integral catalyzer two class catalyzer of second segment form.The feature that the present invention has strong heat release and product ethylene according to direct methane catalytic conversion reaction, ethane is easily oxidized further, proposes the catalyticreactor that a kind of structure is simple, invest low, that energy consumption is low, easy to operate and stable two sections of bed catalysts.The first paragraph of reactor, filling be first time methyl hydride catalyzed conversion pellet type catalyst.And then after having a first time methyl hydride catalyzed conversion reaction, the mixing section of reaction mixture gas delivery of supplemental oxygen voltinism gas.Then be reactor second segment, filling be second time methyl hydride catalyzed conversion integral catalyzer.Reactor bottom is product exit.
Catalyticreactor for realizing aforesaid method provided by the invention, it is characterized in that, this catalyticreactor comprises premixer 3, the first paragraph reactor 4 loading first paragraph catalyzer, oxidizing gas replenisher 6 and loads the second segment reactor 7 of second segment catalyzer, this catalyticreactor top is a pre-mixing chamber 3, pre-mixing chamber 3 is provided with raw material gas inlet 1 and oxidizing gas import 2, what be connected with the lower end of pre-mixing chamber 3 is first paragraph reactor 4, is placed with pellet type catalyst 5 in first paragraph reactor 4; What be connected with first stage reactor 4 lower end is oxidizing gas replenisher 6, oxidizing gas replenisher 6 by be connected with first paragraph reactor 4 and be connected with second segment reactor 7 with first paragraph reactor 4 in isodiametric housing and housing, equally distributed pipe forms, housing is provided with inlet mouth, the diameter of pipe is 0.5-1mm, and it is the hole of 0.1-0.3mm that the centre of pipe has symmetrical, aperture; What be connected with the other end of oxidizing gas replenisher 6 is second segment reactor 7, and second segment reactor 7 is built with integral catalyzer, and the lower end of second segment reactor 7 has product exit 8.
Described reactor, the length-to-diameter ratio of preferred first paragraph reactor 4 and second segment reactor 7 is 1 ~ 3.
Described reactor, preferably wherein the length-to-diameter ratio of oxidizing gas replenisher is 0.1 ~ 0.2.
Temperature of reaction can be provided (known technology equipment) by the heating installation of catalyticreactor shell.
The present invention has following remarkable advantage:
(1) because integral catalyzer has excellent heat and mass transfer performance, catalyticreactor adopts first paragraph to load granular methane catalytic converting catalyst, second segment loads the two-part structure of the methyl hydride catalyzed conversion catalyst of monoblock type, a large amount of reaction heat that can well will produce after first paragraph pellet type catalyst catalyzed conversion methane, and the product ethylene that reaction generates, ethane etc., quickly through second segment integral catalyzer, derive the conversion zone of catalyticreactor, thus while raising methane conversion, avoid the deep oxidation of ethene and ethane, improve the selectivity of ethene and ethane, this is that one-part form catalyticreactor is not accomplished.
(2) between the integral catalyzer of the reactor first paragraph first time pellet type catalyst of methyl hydride catalyzed conversion and the methyl hydride catalyzed conversion of second segment second time, the mixing section of the delivery of supplemental oxygen voltinism gas arranged, after first time methyl hydride catalyzed conversion, in mixed gas, unconverted methane provides again the oxidizing gas of catalyzed conversion, thus improve the one way methane conversion of methyl hydride catalyzed conversion reaction, and then substantially increase the once through yield of ethene and ethane.
(3) the catalyticreactor structure of the methyl hydride catalyzed conversion of the two-part described in ethene processed, ethane is simple, overall craft flow process is short, and operation is stablized, and facility investment is few, the height realizing resource, energy, equipment and flow process is integrated, and then fortifying catalytic reaction process.
Be rich in methane unstripped gas direct method is catalytically conveted to ethene, ethane has following features: in (1) unstripped gas, the content range of methane is wider, and the content of usual methane just has Development volue more than 50%; (2) oxidizing gas is relatively wider, and oxygen, air etc. can use; (3) by product reacted is less, only has a small amount of CO, CO
2, H
2o etc., the polishing purification ratio of ethene and ethane is easier to.Adopt integral catalyzer, can by unconverted methane after the reaction of first paragraph pellet type catalyst, the oxidizing gas provided with delivery of supplemental oxygen voltinism gas mixing chamber carries out catalytic conversion reaction again.Simultaneously, because integral catalyzer has excellent heat and mass transfer performance, can a large amount of reaction heat of producing of methyl hydride catalyzed conversion reaction, and the lower carbon number hydrocarbons such as product ethylene, ethane that reaction generates, the conversion zone of quick derivation catalyticreactor, thus while raising methane conversion, avoid the deep oxidation of ethene and ethane, substantially increase the once through yield of ethene and ethane.
Accompanying drawing explanation
Fig. 1 is catalyticreactor structural representation of the present invention.
Fig. 2 is in catalyticreactor of the present invention, between first paragraph catalyzer and second segment catalyzer, and the mixing section partial schematic diagram of delivery of supplemental oxygen voltinism gas;
1 raw material gas inlet, 2 oxidizing gas imports, 3 pre-mixing chambers, 4 first paragraph reactors, 5 pellet type catalysts, 6 oxidizing gas replenishers, 7 second segment reactors, 8 product exit in above-mentioned accompanying drawing.
Embodiment
Be below detailed description of the present invention, do not form and the present invention is imposed any restrictions.The known technology part that the present invention relates to does not describe in detail, does not also mark in accompanying drawing.In addition, unstripped gas of the present invention can be rich in one or more in the coal-seam gas of methane, Sweet natural gas, biogas, and describing convenient in order to of the present invention, is that unstripped gas is described with coal-seam gas.Those skilled in the art, according to the description of the present embodiment, can understand and adopt other unstripped gas also can complete the present invention.
Catalyzed reaction of the present invention is carried out under 0.1 ~ 1.5MPa pressure condition, and unstripped gas and oxidizing gas are with 1.0 x 10
2~ 5.0 x 10
6h
-1gas space velocity, the gas pre-mixed conjunction room entering catalyticreactor top mixes, and the first paragraph catalyzer then entering catalyticreactor reacts, and temperature of reaction is between 700 DEG C ~ 900 DEG C.In the mixing section of the delivery of supplemental oxygen voltinism gas of reacted gas between first paragraph catalyzer and second segment catalyzer, mix with the oxidizing gas supplemented, then the second segment catalyzer entering catalyticreactor carries out catalytic conversion reaction, product, between 700 DEG C ~ 900 DEG C, is finally drawn catalyticreactor by temperature of reaction.
Catalyticreactor of the present invention is shown in that Fig. 1 is the cylindrical space be made up of metal shell, the top of this catalyticreactor is provided with unstripped gas and oxidizing gas pre-mixing chamber 3, raw material gas inlet 1 and oxidizing gas import 2 is communicated with by pre-mixing chamber 3, the unstripped gas and the oxidizing gas that make to enter catalyticreactor mix, and the first paragraph beaded catalyst then entering catalyticreactor reacts.First paragraph beaded catalyst 5 is Catalyst for Oxidative Coupling of Methane, ethane catalyzer (known technology) at 2 ~ 10mm of particle diameter, if particle diameter is 3 (wt) %Ce/5 (wt) %Na of 3mm
2wO
4-2 (wt) %Mn/SBA-15 pellet type catalyst.
In catalyticreactor of the present invention, between first paragraph catalyzer and second segment catalyzer, the mixing section 6(mixing section partial schematic diagram of a delivery of supplemental oxygen voltinism gas is had to see Fig. 2), it is the cylindrical space identical with catalyticreactor diameter, cylindrical space is the pipe of 0.5 ~ 1mm by diameter, the upper and lower two ends of pipe are communicated with second segment reactor with first paragraph reactor respectively, the centre of pipe has symmetrical, aperture is the hole of 0.1 ~ 0.3mm, by this some holes, oxidizing gas is added in the gas after first paragraph catalyst reaction, and then second segment integral catalyzer 7 is entered.
The second segment integral catalyzer 7 of catalyticreactor of the present invention, monoblock type Catalyst for Oxidative Coupling of Methane, ethane catalyzer, 3 (wt) %Ce/5 (wt) %Na of to be the cordierite honeycomb ceramic of 1mm as adopted channel diameter be monolithic substrate
3pO
4-2 (wt) %Mn/SBA-15/ cordierite monolithic catalyst.This integral catalyzer with pore passage structure, can by unconverted methane after the reaction of first paragraph pellet type catalyst, and the oxidizing gas provided with delivery of supplemental oxygen voltinism gas mixing chamber 6 carries out catalytic conversion reaction again.Simultaneously, because integral catalyzer 7 has excellent heat and mass transfer performance, a large amount of reaction heat that methyl hydride catalyzed conversion reaction can be produced, and product ethylene, ethane that reaction generates, the conversion zone of quick derivation catalyticreactor, thus while raising methane conversion, avoid the deep oxidation of ethene and ethane, substantially increase the once through yield of ethene and ethane.Reaction product, by being located at the product exit 8 bottom catalyticreactor, enters heat reclamation device (known technology).Through the reaction product mixed gas of heat reclamation device, after heat exchange can being carried out by interchanger (known technology) and unstripped gas, oxidizing gas, enter product separation system.
In following table, the first paragraph catalyzer of catalyticreactor used is 3 (wt) %Ce/5 (wt) %Na of particle diameter 3mm
2wO
4-2 (wt) %Mn/SBA-15 pellet type catalyst, second segment catalyzer is 3 (wt) %Ce/5 (wt) %Na
3pO
4-2 (wt) %Mn/SBA-15/ cordierite monolithic catalyst.The length of first paragraph beds is 50mm, diameter 25mm.The length of second segment beds is 50mm, diameter 25mm.The CH of raw material coal-seam gas
4content is 100%, and oxidizing gas material is O
2.Reaction pressure is 0.1MPa, CH
4and O
2total gas space velocity be 3.6 x 10
4h
-1, temperature of reaction is 800 DEG C.Be 3: 1 by the molar ratio of the methane in the unstripped gas of first paragraph pellet type catalyst and the oxygen in oxidizing gas.The molar ratio 3: 0.15 of the methane in first paragraph unstripped gas and supplementary oxygen.
Temperature of reaction is provided (known technology equipment) by the heating installation of catalyticreactor shell.
Table 1 is the coal-seam gas of this example employing and the main component volume content (%) of product
As can be seen from above description, innovative point of the present invention is:
(1) catalyticreactor adopts first paragraph to load granular methane catalytic converting catalyst, second segment loads the two-part structure of the methyl hydride catalyzed conversion catalyst of monoblock type, integral catalyzer is utilized to have excellent heat and mass transfer performance, the a large amount of reaction heat well will produced after first paragraph pellet type catalyst catalyzed conversion methane, and the ethene that reaction generates, the lower carbon number hydrocarbons such as ethane are quickly through second segment integral catalyzer, derive catalyticreactor conversion zone, thus avoid the deep oxidation of ethene and ethane, this is that one-part form catalyticreactor is not accomplished.
(2) between the integral catalyzer of the catalyticreactor first paragraph first time pellet type catalyst of methyl hydride catalyzed conversion and the methyl hydride catalyzed conversion of second segment second time, the mixing section of the delivery of supplemental oxygen voltinism gas arranged, after first time methyl hydride catalyzed conversion, in mixed gas, unconverted methane provides again the oxidizing gas of catalyzed conversion, while raising methane conversion, substantially increase the one way total recovery of ethene and ethane.
(3) the catalyticreactor structure of the methyl hydride catalyzed conversion of the two-part described in ethene processed, ethane is simple, overall craft flow process is short, and operation is stablized, and facility investment is few, the height realizing resource, energy, equipment and flow process is integrated, and then fortifying catalytic reaction process.
Claims (1)
1. the unstripped gas direct catalytic conversion being rich in methane is the method for ethene, ethane by one kind, it is characterized in that, this catalyticreactor comprises premixer, the first paragraph reactor loading first paragraph catalyzer, oxidizing gas replenisher and loads the second segment reactor of second segment catalyzer, this catalyticreactor top is a pre-mixing chamber, pre-mixing chamber is provided with raw material gas inlet and oxidizing gas import, what be connected with the lower end of pre-mixing chamber is first paragraph reactor, is placed with pellet type catalyst in first paragraph reactor; What be connected with first stage reactor lower end is oxidizing gas replenisher, oxidizing gas replenisher by be connected with first paragraph reactor and be connected with second segment reactor with first paragraph reactor in isodiametric housing and housing, equally distributed pipe forms, housing is provided with inlet mouth, the diameter of pipe is 0.5-1mm, and it is the hole of 0.1-0.3mm that the centre of pipe has symmetrical, aperture; What be connected with the other end of oxidizing gas replenisher is second segment reactor, and second segment reactor is built with integral catalyzer, and the lower end of second segment reactor has product exit;
The unstripped gas and the oxidizing gas that are rich in methane during reaction carry out after first time methyl hydride catalyzed conversion reaction through first paragraph pellet type catalyst, in reaction mixture gas, delivery of supplemental oxygen voltinism gas enters second segment integral catalyzer conversion zone again and carries out the methyl hydride catalyzed conversion reaction of second time, last collecting reaction product;
The first paragraph catalyzer of catalyticreactor is 3 (wt) %Ce/5 (wt) %Na of particle diameter 3mm
2wO
4-2 (wt) %Mn/SBA-15 pellet type catalyst, second segment catalyzer is 3 (wt) %Ce/5 (wt) %Na
3pO
4-2 (wt) %Mn/SBA-15/ cordierite monolithic catalyst; The length of first paragraph beds is 50mm, diameter 25mm; The length of second segment beds is 50mm, diameter 25mm; The CH of raw material coal-seam gas
4content is 100%, and oxidizing gas material is O
2; Reaction pressure is 0.1MPa, CH
4and O
2total gas space velocity be 3.6x10
4h
-1, temperature of reaction is 800 DEG C; Reactant gases forms: mole form methane 72.3%, oxygen 24.1%, the molecular fraction 3.6% of supplementary oxygen by the methane in the unstripped gas of first paragraph pellet type catalyst and the oxygen in oxidizing gas.
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Families Citing this family (8)
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| CN107646027A (en) * | 2015-06-08 | 2018-01-30 | 沙特基础全球技术有限公司 | The low entry temperature of methane oxidation coupling |
| CN108025287A (en) * | 2015-06-08 | 2018-05-11 | 沙特基础全球技术有限公司 | Use the methane oxidation coupling of La-Ce catalyst |
| JP2017178885A (en) * | 2016-03-31 | 2017-10-05 | 三菱ケミカル株式会社 | Process for producing hydrocarbon |
| CN111744434B (en) * | 2019-03-27 | 2022-04-22 | 中国石油化工股份有限公司 | Fixed bed reactor for methane oxidative coupling reaction and method for preparing ethylene through methane oxidative coupling |
| CN113769733B (en) * | 2020-06-09 | 2023-12-08 | 中国石油化工股份有限公司 | Catalyst system for preparing carbon dioxide by oxidative coupling of methane and application thereof |
| CN113856666B (en) * | 2020-06-30 | 2024-02-13 | 中国石油化工股份有限公司 | Catalyst system and its use |
| CN115591563B (en) * | 2022-10-08 | 2024-04-23 | 华东师范大学 | Catalyst suitable for fluidized bed methane oxidative coupling reaction and preparation method and application thereof |
| CN116272727B (en) * | 2023-03-10 | 2024-04-05 | 福建德尔科技股份有限公司 | Process and apparatus for producing hexafluoroethane |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2855522Y (en) * | 2005-08-15 | 2007-01-10 | 中国石油化工股份有限公司 | Multi-sectional and fixed-bed type reactor |
| CN101138720A (en) * | 2007-10-19 | 2008-03-12 | 北京化工大学 | Metallic-radicle integral catalyzer for direct catalytic conversion of methyl hydride and method of preparing the same |
| CN101524647A (en) * | 2007-10-19 | 2009-09-09 | 北京化工大学 | Metal base monolithic catalyst for preparing low carbon hydrocarbons by using methane through oxidative coupling and preparation method thereof |
| CN201776133U (en) * | 2010-06-25 | 2011-03-30 | 山东齐旺达集团海仲化工科技有限公司 | Improved low-carbon hydrocarbon aromatization reactor |
| CN102060648A (en) * | 2010-12-30 | 2011-05-18 | 洛阳市科创石化科技开发有限公司 | Method and device for producing propylene and petrol by catalytic pyrolysis of carbon olefins |
-
2012
- 2012-05-16 CN CN201210152674.4A patent/CN102659500B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2855522Y (en) * | 2005-08-15 | 2007-01-10 | 中国石油化工股份有限公司 | Multi-sectional and fixed-bed type reactor |
| CN101138720A (en) * | 2007-10-19 | 2008-03-12 | 北京化工大学 | Metallic-radicle integral catalyzer for direct catalytic conversion of methyl hydride and method of preparing the same |
| CN101524647A (en) * | 2007-10-19 | 2009-09-09 | 北京化工大学 | Metal base monolithic catalyst for preparing low carbon hydrocarbons by using methane through oxidative coupling and preparation method thereof |
| CN201776133U (en) * | 2010-06-25 | 2011-03-30 | 山东齐旺达集团海仲化工科技有限公司 | Improved low-carbon hydrocarbon aromatization reactor |
| CN102060648A (en) * | 2010-12-30 | 2011-05-18 | 洛阳市科创石化科技开发有限公司 | Method and device for producing propylene and petrol by catalytic pyrolysis of carbon olefins |
Non-Patent Citations (1)
| Title |
|---|
| 甲烷氧化偶联催化剂的制备及双层床反应工艺研究;潘登;《中国优秀硕士学位论文全文数据库 工程科技I辑》;20110215;11-15，74-75 * |
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