CN102875288A - Method for producing low-carbon olefins - Google Patents
Method for producing low-carbon olefins Download PDFInfo
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Abstract
The invention relates to a method for producing low-carbon olefins, mainly solving the problem of low yield of low-carbon olefins in the prior art. The method disclosed herein comprises the following steps: (a) contacting a first raw material with a catalyst in a first reaction zone, letting the generated flow and the catalyst enter into a second reaction zone to contact with methanol to generate a product flow and simultaneously form a regeneration catalyst; (b) letting the product flow and the regeneration catalyst enter into a depression stripper, letting a part of the separated regeneration catalyst return to the second reaction zone, and letting the other part of the separated regeneration catalyst enter into a regenerator for regenerating to form a regenerated catalyst; (c) letting a part of the regenerated catalyst enter into the first reaction zone, letting another part of the regenerated catalyst enter into a third reaction zone to contact with a second raw material, and letting the generated product flow and the catalyst enter into the depression stripper, wherein the ratio of the length of time in the first reaction zone to the length of time in the second reaction zone is 1.5-5:1, and the first raw material is C4-C7 hydrocarbon separated by a separation segment. The method disclosed herein well solves the problem and can be applied in the industrial production of low-carbon olefins.
Description
Technical field
The present invention relates to a kind of method of producing low-carbon alkene, the method for especially producing low-carbon alkene by methyl alcohol and light naphthar.
Technical background
Low-carbon alkene, namely ethene and propylene are two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but because limited supply and the higher price of petroleum resources, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people begin to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials that is used for light olefin production of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, such as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize up to a million tonnes industrial scale.Because the popularity in oxygenatedchemicals source, add and transform the economy that generates light olefin technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), particularly the technique by preparing olefin by conversion of methanol (MTO) is subject to increasing attention.
Petroleum naphtha is a kind of light-end products, is cut corresponding cut and is got by crude distillation or oil secondary processing.Its boiling spread is decided according to need, is generally wider boiling range, such as 20-220 ℃.Petroleum naphtha is the pyrolysis in tubular furnace preparing ethylene, and propylene and catalytic reforming are produced the important source material of benzene,toluene,xylene.As cracking stock, require petroleum naphtha form in the content of alkane and naphthenic hydrocarbon be not less than 70% (volume).The naphtha catalytic pyrolysis preparing low-carbon alkene then is under the condition that catalyzer exists, and petroleum hydrocarbon is carried out the production process that cracking obtains low-carbon alkene.Compare with traditional tube furnace steam heat cracking, this process reaction temperature is than approximately low 50～200 ℃ of steam cracking reactions, and energy consumption significantly reduces; Cracking furnace pipe inwall coking rate also can reduce, thereby but prolong operation cycle increases the boiler tube life-span; Simultaneously Carbon emission also can reduce, and has alleviated pollution, and can adjust the product mix flexibly.
Technology and reactor that a kind of oxygenate conversion is low-carbon alkene have been announced among the US6166282, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu reaction of gas speed is finished, after rising to the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Because reaction after product gas and catalyzer sharp separation have effectively prevented the generation of secondary reaction.Through analog calculation, to compare with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.
The multiple riser reaction unit of having announced among the CN1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises a plurality of riser reactors, gas solid separation district, a plurality of offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and gas product are separated.But there is the lower shortcoming of yield of light olefins in the method.
Announced a kind of method of methanol production propylene among EP0448000 and the EP0882692, methyl alcohol at first is converted into DME and water, then mixture is transported to the First reactor, and adds steam in this reactor.In the first reactor methyl alcohol with (or) dme or its mixture contact with catalyzer and react, catalyzer adopts the special-purpose ZSM-5 catalyzer that contains ZnO and CdO, 280～570 ℃ of temperature of reaction, pressure 0.01～0.1MPa prepares the product take propylene as main hydro carbons.Heavier product such as C
5 +The hydrocarbon continuation is reacted in second reactor and is converted into take propylene as main hydro carbons, sends separator back to after cooling.Product is compressed, can obtain purity after further refining is 97% chemical grade propylene.But adopt a plurality of fixed-bed reactor in this technique, because the restriction of the activity of catalyzer therefore need frequent blocked operation, and the heat-obtaining problem is also very complicated.
US 20070083071 has announced the processing method that a kind of hydrocarbon catalytic pyrolysis is produced ethene, propylene, hydrocarbon feed is converted into the product that comprises low-carbon alkene in catalytic cracker, then product stream is separated into C2～C3 alkane, C2～C3 alkene, three kinds of logistics of C4+ hydrocarbon by series of process, C2～C3 alkane is returned tube cracking furnace carry out thermo-cracking, the C4+ hydrocarbon returns catalytic cracker and carries out catalytic pyrolysis, finally obtains ethene, the propylene product of higher yields.The method adopts riser reactor, and reactant residence time is shorter, and low-carbon alkene product once through yield is lower.
Since the reaction of naphtha catalytic cracking and preparing olefin by conversion of methanol the purpose product---low-carbon alkene is identical, and the main ingredient kind in the product is roughly the same separately, the catalyst system that adopts is also roughly the same, and from the reaction mechanism angle, all have the process that is cracked into the small molecules hydro carbons by macromole hydrocarbon or intermediate, so these two kinds of Technologies are had ready conditions and are coupled.How these two kinds of Technologies are coupled, then how improving yield of light olefins is two more scabrous problems.The present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the lower problem of yield of light olefins that exists in the prior art, and a kind of method of new production low-carbon alkene is provided.The method is used for the production of low-carbon alkene, has advantages of that yield of light olefins is higher.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of method of producing low-carbon alkene, said method comprising the steps of: (a) the first raw material contacts with molecular sieve catalyst in the first reaction zone, the product stream and the catalyzer that generate enter second reaction zone together, contact with 60～150 ℃ methyl alcohol, generation comprises the product stream of low-carbon alkene, forms simultaneously reclaimable catalyst; (b) described product stream and reclaimable catalyst enter the sedimentation stripper that is positioned at the revivifier top, enter centrifugal station through the product stream after the gas solid separation, isolated reclaimable catalyst returns second reaction zone through the stripping rear portion, a part enters revivifier regeneration by regeneration standpipe, forms regenerated catalyst; (c) described regenerated catalyst enters the first reaction zone through degassed rear portion, a part enters the 3rd reaction zone that is built in the revivifier, contact with the second raw material that is mainly petroleum naphtha, generation comprises that the product stream of low-carbon alkene and catalyzer enter the sedimentation stripper together; Wherein, described regenerated catalyst activity index is greater than 0.8, and second reaction zone and the first reaction zone gas phase residence time are that 1.5～5: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station.
In the technique scheme, described molecular sieve comprises ZSM-5, SiO
2/ Al
2O
3Mol ratio is 10～100; Described the first reaction zone is riser tube, and described second reaction zone is turbulence or fast fluidized bed, and described the 3rd reaction zone is riser tube; The riser tube quantity of described the 3rd reaction zone is at least 1; Stripping medium and degassed medium are water vapour; Reaction conditions is in described the first reaction zone: temperature of reaction is 550～650 ℃, and the gas phase linear speed is 5～10 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 470～550 ℃, and the gas phase linear speed is 0.8～3.0 meter per second; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 580～680 ℃, and the gas phase linear speed is 5～10 meter per seconds; Described isolated reclaimable catalyst 40～70% weight behind stripping are returned second reaction zone, and 30～60% weight enter revivifier regeneration by regeneration standpipe; Described regenerated catalyst 40～65% weight after degassed enter the first reaction zone, and 35～60% weight enter the 3rd reaction zone that is built in the revivifier.
Adopt method of the present invention, three reaction zones are set, it is low-carbon alkene that the 3rd reaction zone is mainly used in the light naphthar catalytic pyrolysis, second reaction zone is mainly used in methanol oxidation and is converted into low-carbon alkene, and the first reaction zone is mainly used in transforming carbon four～carbon seven hydrocarbon that form in first, second reaction zone, this part carbon four～carbon seven hydrocarbon comprises the carbon four above hydrocarbon that light naphthar and methanol conversion generate, and also comprises the unconverted light naphthar of part.This just is further converted to low-carbon alkene with some by product that light naphthar, methanol conversion generate, and has improved the yield of low-carbon alkene.In addition, adopt the first reaction zone to connect with second reaction zone among the present invention, gas phase in the first reaction zone comprises low-carbon alkene, high-carbon hydrocarbon, after entering second reaction zone, methyl alcohol is as the source that methyl is provided, can be low-carbon alkene by the hydro carbons in the further conversion system of the reactions such as autocatalysis, thereby reach the purpose that improves yield of light olefins.
Adopt technical scheme of the present invention: described molecular sieve comprises ZSM-5, SiO
2/ Al
2O
3Mol ratio is 10～100; Described the first reaction zone is riser tube, and described second reaction zone is turbulence or fast fluidized bed, and described the 3rd reaction zone is riser tube; The riser tube quantity of described the 3rd reaction zone is at least 1; Stripping medium and degassed medium are water vapour; Reaction conditions is in described the first reaction zone: temperature of reaction is 550～650 ℃, and the gas phase linear speed is 5～10 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 470～550 ℃, and the gas phase linear speed is 0.8～3.0 meter per second; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 580～680 ℃, and the gas phase linear speed is 5～10 meter per seconds; Described isolated reclaimable catalyst 40～70% weight behind stripping are returned second reaction zone, and 30～60% weight enter revivifier regeneration by regeneration standpipe; Described regenerated catalyst 40～65% weight after degassed enter the first reaction zone, and 35～60% weight enter the 3rd reaction zone that is built in the revivifier, and the low-carbon alkene carbon base absorption rate can reach 63.54% (weight), has obtained preferably technique effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is regeneration air feed; 2 is the regeneration standpipe flowrate control valve; 3 is the first reaction zone feeds; 4 is buffer zone; 5 is degassed medium charging; 6 is regenerator sloped tube; 7 is degassing vessel; 8 is the first reaction zone; 9 is the second reaction zone charging; 10 is second reaction zone; 11 is regeneration standpipe; 12 return the revivifier pipeline for the degassing vessel gas phase; 13 is revivifier; 14 is the charging of stripping medium; 15 is gas-solid cyclone separator; 16 is the regenerated flue gas outlet line; 17 are the sedimentation stripper; 18 is stripping zone; 19 is second reaction zone catalyst recirculation pipe; 20 is gas-solid cyclone separator; 21 is the product gas outlet pipeline; 22 is the second raw material charging; 23 is the degassed medium inlet of built-in degas zone; 24 is built-in degas zone; 25 is the 3rd reaction zone.
The first raw material enters in the first reaction zone 8 through feeding line 3, contact with molecular sieve catalyst, the product that reaction generates carries catalyzer and enters in the second reaction zone 10, generate low-carbon alkene product and carbon deposition catalyst and enter sedimentation stripping zone 17, carbon deposition catalyst is through entering revivifier 13 regeneration by regeneration standpipe 11 behind the stripping, catalyzer part after the regeneration is returned the first reaction zone 8 through regenerator sloped tube 6, a part enters the 3rd built-in reaction zone 25, contact with the second raw material, in the product introduction sedimentation stripper 17 that generates, enter centrifugal station from product gas outlet pipeline 21.
The invention will be further elaborated below by embodiment, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In reaction-regenerative device as shown in Figure 1, catalyzer is ZSM-5, SiO
2/ Al
2O
3Mol ratio is 100, and the binding agent mass content is 55% in the catalyzer, and binding agent is SiO
2The ZSM-5 molecular sieve mass content is 45%, the revivifier medial temperature is 654 ℃, the spent agent carbon deposition quantity is 3.5% (weight), the regenerated catalyst carbon deposition quantity is 0.15% (weight), the sedimentation stripper is positioned at revivifier top, stripping zone is built in the revivifier, the first reaction zone is riser tube, and second reaction zone is fast fluidized bed, and the 3rd reaction zone is 1 riser tube, the light naphthar composition of the 3rd reaction zone feeds sees Table 1, and adding water vapour as thinner, the mass ratio of water vapour and light naphthar is 0.5: 1, with the light naphthar parallel feeding.The methanol feeding temperature is 60 ℃.The regenerated catalyst activity index is 0.91, second reaction zone and the first reaction zone gas phase residence time are 5: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station, stripping medium and degassed medium are water vapour, reaction conditions is in the first reaction zone: temperature of reaction is 550 ℃, and the gas phase linear speed is 5 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 470 ℃, and the gas phase linear speed is 0.8 meter per second; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 580 ℃, the gas phase linear speed is 5 meter per seconds, isolated reclaimable catalyst 70% weight behind stripping is returned second reaction zone, 30% weight enters revivifier regeneration by regeneration standpipe, regenerated catalyst 40% weight after degassed enters the first reaction zone, and 60% weight enters two the 3rd reaction zones that are built in the revivifier.The weight ratio of methyl alcohol and light naphthar charging is 1: 1, keeps the stability of catalyst flow control, and gas product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 60.21% weight.
Table 1 petroleum naphtha the typical case form
| Initial boiling point, ℃ | 40 |
| Final boiling point, ℃ | 162 |
| Positive structure and isoparaffin, % by weight | 65.18 |
| Alkene, % by weight | 0.17 |
| Naphthenic hydrocarbon, % by weight | 28.44 |
| Aromatic hydrocarbons, % by weight | 6.21 |
[embodiment 2]
According to embodiment 1 described condition and step, catalyzer adopts ZSM-5, SiO
2/ Al
2O
3Mol ratio is 10, the revivifier medial temperature is 674 ℃, the spent agent carbon deposition quantity is 3.2% (weight), the regenerated catalyst carbon deposition quantity is 0.03% (weight), the sedimentation stripper is positioned at revivifier top, stripping zone is built in the revivifier, the first reaction zone is riser tube, second reaction zone is turbulent fluidized bed, the 3rd reaction zone is the riser tube of 2 same sizes, also add water vapour in the light naphthar of the 3rd reaction zone feeds as thinner, the mass ratio of water vapour and light naphthar is 1: 1, with the light naphthar parallel feeding.The methanol feeding temperature is 150 ℃.The regenerated catalyst activity index is 0.96, second reaction zone and the first reaction zone gas phase residence time are 1.5: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station, stripping medium and degassed medium are water vapour, reaction conditions is in the first reaction zone: temperature of reaction is 650 ℃, and the gas phase linear speed is 10 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 550 ℃, and the gas phase linear speed is 3.0 meter per seconds; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 679 ℃, the gas phase linear speed is 10 meter per seconds, isolated reclaimable catalyst 40% weight behind stripping is returned second reaction zone, 60% weight enters revivifier regeneration by regeneration standpipe, regenerated catalyst 65% weight after degassed enters the first reaction zone, and 35% weight enters the 3rd reaction zone that is built in the revivifier.The weight ratio of methyl alcohol and light naphthar charging is 1: 2, keeps the stability of catalyst flow control, and gas product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 55.36% weight.
[embodiment 3]
According to embodiment 1 described condition and step, catalyzer adopts ZSM-5, SiO
2/ Al
2O
3Mol ratio is 50, the revivifier medial temperature is 680 ℃, the spent agent carbon deposition quantity is 3.9% (weight), the regenerated catalyst carbon deposition quantity is 0.33% (weight), the sedimentation stripper is positioned at revivifier top, stripping zone is built in the revivifier, the first reaction zone is riser tube, second reaction zone is turbulent fluidized bed, the 3rd reaction zone is 1 riser tube, also add water vapour in the light naphthar of the 3rd reaction zone feeds as thinner, the mass ratio of water vapour and light naphthar is 1: 1, with the light naphthar parallel feeding.The methanol feeding temperature is 120 ℃.The regenerated catalyst activity index is 0.81, second reaction zone and the first reaction zone gas phase residence time are 2: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station, stripping medium and degassed medium are water vapour, reaction conditions is in the first reaction zone: temperature of reaction is 630 ℃, and the gas phase linear speed is 7 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 500 ℃, and the gas phase linear speed is 2.0 meter per seconds; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 653 ℃, the gas phase linear speed is 6 meter per seconds, isolated reclaimable catalyst 50% weight behind stripping is returned second reaction zone, 50% weight enters revivifier regeneration by regeneration standpipe, regenerated catalyst 50% weight after degassed enters the first reaction zone, and 50% weight enters the 3rd reaction zone that is built in the revivifier.The weight ratio of methyl alcohol and light naphthar charging is 2: 1, keeps the stability of catalyst flow control, and gas product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 63.54% weight.
[embodiment 4]
According to embodiment 1 described condition and step, catalyzer adopts ZSM-5, SiO
2/ Al
2O
3Mol ratio is 30, the revivifier medial temperature is 650 ℃, the spent agent carbon deposition quantity is 2.8% (weight), the regenerated catalyst carbon deposition quantity is 0.13% (weight), the sedimentation stripper is positioned at revivifier top, stripping zone is built in the revivifier, the first reaction zone is riser tube, second reaction zone is turbulent fluidized bed, the 3rd reaction zone is 1 riser tube, also add water vapour in the light naphthar of the 3rd reaction zone feeds as thinner, the mass ratio of water vapour and light naphthar is 0.5: 1, with the light naphthar parallel feeding.The methanol feeding temperature is 140 ℃.The regenerated catalyst activity index is 0.89, second reaction zone and the first reaction zone gas phase residence time are 2: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station, stripping medium and degassed medium are water vapour, reaction conditions is in the first reaction zone: temperature of reaction is 620 ℃, and the gas phase linear speed is 6 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 486 ℃, and the gas phase linear speed is 1.5 meter per seconds; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 628 ℃, the gas phase linear speed is 5 meter per seconds, isolated reclaimable catalyst 50% weight behind stripping is returned second reaction zone, 50% weight enters revivifier regeneration by regeneration standpipe, regenerated catalyst 50% weight after degassed enters the first reaction zone, and 50% weight enters the 3rd reaction zone that is built in the revivifier.The weight ratio of methyl alcohol and light naphthar charging is 1: 1, keeps the stability of catalyst flow control, and gas product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 58.71% weight.
[comparative example 1]
According to embodiment 1 described condition and step, do not establish the first reaction zone, the low-carbon alkene carbon base absorption rate is 51.08% weight.
Obviously, adopt method of the present invention, can reach the purpose that improves yield of light olefins, have larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (7)
1. method of producing low-carbon alkene may further comprise the steps:
(a) the first raw material contacts with molecular sieve catalyst in the first reaction zone, and the product stream of generation and catalyzer enter second reaction zone together, contacts with 60～150 ℃ methyl alcohol, generates the product stream that comprises low-carbon alkene, forms simultaneously reclaimable catalyst;
(b) described product stream and reclaimable catalyst enter the sedimentation stripper that is positioned at the revivifier top, enter centrifugal station through the product stream after the gas solid separation, isolated reclaimable catalyst returns second reaction zone through the stripping rear portion, a part enters revivifier regeneration by regeneration standpipe, forms regenerated catalyst;
(c) described regenerated catalyst enters the first reaction zone through degassed rear portion, a part enters the 3rd reaction zone that is built in the revivifier, contact with the second raw material that is mainly petroleum naphtha, generation comprises that the product stream of low-carbon alkene and catalyzer enter the sedimentation stripper together;
Wherein, described regenerated catalyst activity index is greater than 0.8, and second reaction zone and the first reaction zone gas phase residence time are that 1.5～5: 1, the first raw material is mainly isolated carbon four～carbon seven hydrocarbon of described centrifugal station.
2. the method for described production low-carbon alkene according to claim 1 is characterized in that described molecular sieve comprises ZSM-5, SiO
2/ Al
2O
3Mol ratio is 10～100; Described the first reaction zone is riser tube, and described second reaction zone is turbulence or fast fluidized bed, and described the 3rd reaction zone is riser tube.
3. the method for described production low-carbon alkene according to claim 1 is characterized in that the riser tube quantity of described the 3rd reaction zone is at least 1.
4. the method for described production low-carbon alkene according to claim 1 is characterized in that stripping medium and degassed medium are water vapour.
5. the method for described production low-carbon alkene according to claim 1, it is characterized in that reaction conditions is in described the first reaction zone: temperature of reaction is 550～650 ℃, the gas phase linear speed is 5～10 meter per seconds; Reaction conditions is in the second reaction zone: temperature of reaction is 470～550 ℃, and the gas phase linear speed is 0.8～3.0 meter per second; Reaction conditions is in the 3rd reaction zone: temperature of reaction is 580～680 ℃, and the gas phase linear speed is 5～10 meter per seconds.
6. the method for described production low-carbon alkene according to claim 1 is characterized in that described isolated reclaimable catalyst 40～70% weight behind stripping return second reaction zone, and 30～60% weight enter revivifier regeneration by regeneration standpipe.
7. the method for described production low-carbon alkene according to claim 1 is characterized in that described regenerated catalyst 40～65% weight after degassed enter the first reaction zone, and 35～60% weight enter the 3rd reaction zone that is built in the revivifier.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478648A (en) * | 2014-12-30 | 2015-04-01 | 江苏健神生物农化有限公司 | Method for preparing light olefins through catalytic pyrolysis by adopting naphtha as raw material |
| CN111606771A (en) * | 2020-06-11 | 2020-09-01 | 中国石油化工股份有限公司 | Methanol and light hydrocarbon coupling cracking device and method |
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| CN101279877A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for increasing yield of ethylene and propone in conversion process of oxocompound |
| CN101955406A (en) * | 2009-07-20 | 2011-01-26 | 中国科学院大连化学物理研究所 | Method for producing propylene and ethylene byproduct |
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| CN101130469A (en) * | 2006-08-23 | 2008-02-27 | 中国科学院大连化学物理研究所 | Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol |
| CN101279877A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for increasing yield of ethylene and propone in conversion process of oxocompound |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104478648A (en) * | 2014-12-30 | 2015-04-01 | 江苏健神生物农化有限公司 | Method for preparing light olefins through catalytic pyrolysis by adopting naphtha as raw material |
| CN111606771A (en) * | 2020-06-11 | 2020-09-01 | 中国石油化工股份有限公司 | Methanol and light hydrocarbon coupling cracking device and method |
| CN111606771B (en) * | 2020-06-11 | 2022-09-23 | 中国石油化工股份有限公司 | Methanol and light hydrocarbon coupling cracking device and method |
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