CN101045666A - Method for producing propene ethylene by carbon-contained alkene - Google Patents
Method for producing propene ethylene by carbon-contained alkene Download PDFInfo
- Publication number
- CN101045666A CN101045666A CNA2006100251077A CN200610025107A CN101045666A CN 101045666 A CN101045666 A CN 101045666A CN A2006100251077 A CNA2006100251077 A CN A2006100251077A CN 200610025107 A CN200610025107 A CN 200610025107A CN 101045666 A CN101045666 A CN 101045666A
- Authority
- CN
- China
- Prior art keywords
- carbon
- reaction
- ethylene
- producing propene
- alkene
- 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.)
- Granted
Links
Images
Classifications
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for preparing propene or ethene from C-contained olefin includes such steps as heating raw material by heat exchange with cracked product, heating to reaction temp by heater, cracking reaction at 400-600 deg.C under 10-50 KPa, heat exchange between cracked product and raw material, condensing to separate out C5 or more fraction, compressing, and separating propene or ethene.
Description
Technical field
The present invention relates to a kind of method of producing propene ethylene by carbon-contained alkene.
Background technology
Propylene, ethene are one of important basic Organic Chemicals.Propylene is mainly used in many products such as producing PP, isopropyl benzene, vinyl cyanide, vinylformic acid; Ethene is the main raw material of producing polyethylene (PE), polyvinyl chloride (PVC) and ethylene oxide/ethylene glycol important organic chemical industry's products such as (EO/EG).As important light olefin, propylene, ethene year demand in continuous growth.Hydrocarbon pyrolysis is still one of main method of producing ethene, but and the general overview of the technology of production propylene is byproduct technology and proprietary technology.Byproduct technology mainly is meant the propylene that obtains by steam cracking and catalytic cracking system ethylene unit.Proprietary technology refers to the technology of special Development and Production propylene, mainly contains Technologies such as dehydrogenating propane, low-carbon alkene disproportionation, low-carbon alkene cracking, preparing propylene from methanol at present.Low-carbon alkene cracking system propylene technology not only can be used for producing propylene, ethene, and can improve the added value of low-carbon alkene, has very big development prospect.The ultimate principle of low-carbon alkene preparing propylene by catalytic cracking technology is to utilize to have uniqueness and select type and tart ZSM-5 molecular sieve catalyst, selectively low-carbon alkene is cracked into propylene and ethene.
Document WO 2004096439 has been introduced a kind of technology of mixed olefins cracking system light olefin.This technology does not adopt shared material, and the raw material mixed olefins carries out scission reaction under the high-speed condition.This technology can obtain multiple light olefin, but very not high to propylene, selectivity of ethylene.
Document EP 109059 has been introduced a kind of C
4～C
12The technology of mixed olefins system propylene, ethene, this technology does not have shared material equally, and the raw material mixed olefins is directly greater than 50 hours
-1Weight space velocity under carry out scission reaction.This production technique is not very high to the selectivity of propylene, and to C
5The selectivity of above cut is on the contrary greater than 33%.
The described technology of above-mentioned document all is under the condition that does not need shared material mixed olefins to be carried out cracking, produces propylene and ethylene.But, because scission reaction is to carry out under positive pressure, so olefin conversion and all can not be very high to propylene, selectivity of ethylene.
Summary of the invention
Technical problem to be solved by this invention is C in the conventional art
4～C
8Carbonaceous olefin mixture is converted into C
2～C
3The problem that olefin yields is low provides a kind of method of new producing propene ethylene by carbon-contained alkene.This method has when carbonaceous olefin mixture carried out catalytic cracking reaction, obtains the advantage of high yield propylene, cracking of ethylene product.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of producing propene ethylene by carbon-contained alkene may further comprise the steps:
(1) gasification and preheating after liquid phase feed carbonaceous olefin and the split product heat exchange is heated to 400～600 ℃ then, enters reactor and carries out catalytic cracking reaction;
(2) catalytic cracking reaction is to carry out under 10～50Kpa condition in absolute pressure;
(3) with the heat exchange of raw material carbonaceous olefin after split product, after condensation, enter knockout drum; The gas-liquid separation pot bottom is isolated liquid phase C
5Above cut, top portion enters the later separation device after the vapor-phase thermal cracking product that obtains is by compressor compresses, separate to obtain propylene, ethene.
In the technique scheme, the carbon-contained alkene by catalytic cracking preferred catalyst is the type ZSM 5 molecular sieve catalyzer; Reacting used liquid phase feed preferred version is C
4～C
8Carbonaceous olefin mixture; The reaction feed preferred version enters reactor and carries out catalytic cracking reaction for being heated to 450～550 ℃; Reaction weight space velocity preferable range is 5～100 hours in the reactor
-1, more preferably scope is 5～50 hours
-1Reaction absolute pressure preferable range is 15～40KPa in the reactor.Split product temperature preferable range after condensation is 10～80 ℃, and more preferably scope is 20～60 ℃.The preferred version of reacting system pressure is to be produced by compressor.
Propylene that the inventive method obtains and ethene are no less than 60% of alkene total amount in the raw material.The catalytic cracking reaction of the inventive method is to carry out under negative pressure, has improved in the raw material conversion of olefines rate and to propylene, selectivity of ethylene, has obtained more propylene, ethene.If be incorporated into preparing ethylene by steam cracking device, FCC apparatus and other propylene enhancing device such as preparing propylene from methanol device, then present method can obtain highly purified propylene, ethene, has obtained better technical effect.
Description of drawings
Fig. 1 is the inventive method process flow diagram;
Fig. 2 is document EP 109059 process flow diagrams;
1 is the raw material carbonaceous olefin mixture among Fig. 1 or Fig. 2, and 2 is process furnace, and 3 is reactor, and 4 is feed exchanger, and 5 is fractional distillating tube, and 6 is gas-liquid separator, and 7 is compressor, and 8 is the vapor-phase thermal cracking product, and 9 is C
5Above cut, 10 is C
2Following cut, 11 is C
3Cut, 12 is other cut, 13 is mixed C
4～C
8
Among Fig. 1, carbonaceous olefin mixture 1 and reactor pyrolysis product be in heat exchanger 4 heat exchange, after gasification, the preheating again through adding Hot stove 2 is heated to reaction temperature. The reactor pyrolysis product is after heat exchanger 4 heat exchange, again through fractional distilling tube 5 partial condensations After enter knockout drum 6. Gas-liquid separator 6 bottom liquid phases 9 are C5Above cut. Gas-liquid separator 6 top gas phase warps Enter the later separation device after compressor 7 compressions, obtain propylene, ethene.
The invention will be further elaborated below by embodiment.
Embodiment
[comparative example 1]
By shown in Figure 2, carbonaceous olefin mixture is formed (weight %) and is: iso-butylene: 45%, and Trimethylmethane: 55%.Adopt document EP 109059 technical process, weight hourly space velocity is 80 hours
-1, temperature of reaction is 575 ℃, and reaction pressure is 0.05MPa, and the catalytic cracking reaction catalyzer is SiO
2And Al
2O
3Mol ratio is 300 ZSM-5 molecular sieve, experimental results show that the product (weight %) that will obtain following ratio:
C
2Alkene: 0.11%
C
3Alkene: 23.3%
C
4：28.5％
C
5More than: 48.09%
[comparative example 2]
By shown in Figure 2, carbonaceous olefin mixture is formed (weight %) and is: iso-butylene: 45%, and Trimethylmethane: 55%.Adopt document EP 109059 technical process, weight hourly space velocity 60 hours
-1, temperature of reaction is 550 ℃, and reaction pressure is 0.15MPa, and the catalytic cracking reaction catalyzer is SiO
2And Al
2O
3Mol ratio is 300 ZSM-5 molecular sieve, and evidence will obtain the product (weight %) of following ratio:
C
2Alkene: 0.07%
C
3Alkene: 34.11%
C
4：18.25％
C
5More than: 47.64%
[embodiment 1]
By shown in Figure 1, carbonaceous olefin mixture is formed (weight %) and is: iso-butylene: 45%, and Trimethylmethane: 55%.Adopt technical process of the present invention, catalyzer is that silica alumina ratio is 200 ZSM-5 molecular sieve, and the reaction weight hourly space velocity is 10 hours
-1, temperature of reaction is 450 ℃, and reaction pressure is 15KPa (absolute pressure), and the temperature behind the fractional distillating tube 5 is 25 ℃, and the pilot plant proof will obtain the product (relative and raw material olefin content) of following ratio:
C
2～C
3：68.3％
Fuel gas: 0.08%
C
4Above cut: 31.6%
[embodiment 2]
By shown in Figure 1, carbonaceous olefin mixture is formed with embodiment 1.Adopt technical process of the present invention, catalyzer is that silica alumina ratio is 200 ZSM-5 molecular sieve, and the reaction weight hourly space velocity is 80 hours
-1, temperature of reaction is 500 ℃, and reaction pressure is 30KPa (absolute pressure), and the temperature behind the fractional distillating tube 5 is 45 ℃, will obtain the product (weight %) of following ratio:
C
2～C
3：65.5％
Fuel gas: 0.07%
C
4Above cut: 34.4%
[embodiment 3]
By shown in Figure 1, carbonaceous olefin mixture is formed with embodiment 1.Adopt technical process of the present invention, catalyzer is that silica alumina ratio is 200 ZSM-5 molecular sieve, and the reaction weight hourly space velocity is 30 hours
-1, temperature of reaction is 550 ℃, and reaction pressure is 50KPa (absolute pressure), and the temperature behind the fractional distillating tube 5 is 55 ℃, will obtain the product (weight %) of following ratio:
C
2～C
3：69.5％
Fuel gas: 0.1%
C
4Above cut: 30.4%
Claims (9)
1, a kind of method of producing propene ethylene by carbon-contained alkene may further comprise the steps:
(1) gasification and preheating after liquid phase feed carbonaceous olefin and the split product heat exchange is heated to 400～600 ℃ then, enters reactor and carries out catalytic cracking reaction;
(2) catalytic cracking reaction is to carry out under 10～50KPa in absolute pressure;
(3) with the heat exchange of raw material carbonaceous olefin after split product, after condensation, enter knockout drum; The gas-liquid separation pot bottom is isolated liquid phase C
5Above cut, top portion enters the later separation device after the vapor-phase thermal cracking product that obtains is by compressor compresses, separate to obtain propylene, ethene.
2, according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1, it is characterized in that reacting used liquid phase feed is C
4～C
8Carbonaceous olefin mixture; Reaction feed is heated to 450～550 ℃, enters reactor and carries out catalytic cracking reaction.
3,, it is characterized in that the reaction weight space velocity is 5～100 hours in the reactor according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1
-1
4,, it is characterized in that the reaction weight space velocity is 5～50 hours in the reactor according to the method for the described producing propene ethylene by carbon-contained alkene of claim 3
-1
5,, it is characterized in that the reaction absolute pressure is 15～40KPa in the reactor according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1.
6,, it is characterized in that system's negative pressure is produced by compressor according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1.
7,, it is characterized in that split product temperature after condensation is 10～80 ℃ according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1.
8,, it is characterized in that split product temperature after condensation is 20～60 ℃ according to the method for the described producing propene ethylene by carbon-contained alkene of claim 7.
9,, it is characterized in that the catalytic cracking reaction catalyst system therefor is a type ZSM 5 molecular sieve according to the method for the described producing propene ethylene by carbon-contained alkene of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100251077A CN100522900C (en) | 2006-03-27 | 2006-03-27 | Method for producing propene ethylene by carbon-contained alkene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100251077A CN100522900C (en) | 2006-03-27 | 2006-03-27 | Method for producing propene ethylene by carbon-contained alkene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101045666A true CN101045666A (en) | 2007-10-03 |
| CN100522900C CN100522900C (en) | 2009-08-05 |
Family
ID=38770613
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100251077A Active CN100522900C (en) | 2006-03-27 | 2006-03-27 | Method for producing propene ethylene by carbon-contained alkene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100522900C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111019689A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019688A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019691A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019690A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111117704A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Method and device for preparing low-carbon olefin from petroleum hydrocarbon |
-
2006
- 2006-03-27 CN CNB2006100251077A patent/CN100522900C/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111019689A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019688A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019691A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019690A (en) * | 2018-10-10 | 2020-04-17 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019691B (en) * | 2018-10-10 | 2022-03-15 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019690B (en) * | 2018-10-10 | 2022-03-29 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111019689B (en) * | 2018-10-10 | 2022-03-29 | 中国石油化工股份有限公司 | Low-carbon olefin cracking equipment and cracking method |
| CN111117704A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Method and device for preparing low-carbon olefin from petroleum hydrocarbon |
| CN111117704B (en) * | 2018-10-30 | 2021-08-03 | 中国石油化工股份有限公司 | Method and device for preparing low-carbon olefin from petroleum hydrocarbon |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100522900C (en) | 2009-08-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101092323B (en) | Method for preparing olefin in lightweight by catalytic cracking olefin of containing carbon | |
| CN1194957C (en) | Process for the simultaneous coproduction and purification of ethyl acetate and isopropyl acetate | |
| RU2747308C1 (en) | In-situ method for obtaining catalyst for obtaining at least one of toluene, para-xylol and lower olefins as well as reaction process | |
| JP5870028B2 (en) | Method and system for producing isoprene | |
| CN101279879A (en) | Method for producing propone by comprehensive utilization of mixed C4 | |
| CN101045666A (en) | Method for producing propene ethylene by carbon-contained alkene | |
| CN1805914A (en) | Process for production of propylene and ethylbenzene from dilute ethylene streams | |
| CN1102562C (en) | Olefin skeletal isomerization process | |
| CN100506761C (en) | Method for producing propylene ethane by catalytic cracking carbon-containing olefin | |
| CN101045665A (en) | Method for producing propylene from carbon-contained alkene by catalytic cracking | |
| CN100418938C (en) | Method for separating product of carbonaceous olefin catalytic cracking | |
| CN1264799C (en) | Process for producing (meth)acrylic acid | |
| CN100506760C (en) | Method for producing propylene ethane by carbon-containing olefin catalytic cracking | |
| CN1029309C (en) | New aromatic alkylation process | |
| CN103420752B (en) | Separation refinement method for ethylene preparation through biomass ethanol dehydration | |
| CN102070390A (en) | Method for preparing propylene from refinery mixed C4 | |
| CN1239444C (en) | Isoalkene producing process | |
| CN103772102B (en) | The separation and refining method of producing ethylene from dehydration of ethanol | |
| CN100430352C (en) | Method for separating carbon-containing olefin cracked product | |
| CN1230405C (en) | Method for producing ethyl benzene | |
| CN1927782A (en) | Method for increasing production of propylene and ethylene by catalytic cracking carbonaceous olefin mixture | |
| CN1258509C (en) | Method for the hydroformylation of olefins with 2 to 6 carbon atoms | |
| CN214270725U (en) | Device for comprehensively utilizing mixed carbon four | |
| CN1151106C (en) | Olefine-arene reaction process of preparing alkyl arene | |
| CN1927781A (en) | Method of preparing light olefin by catalytic cracking carbonaceous olefin mixture |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |