CN104250193A - Preparation method of propylene and butadiene - Google Patents
Preparation method of propylene and butadiene Download PDFInfo
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Abstract
The invention discloses a preparation method of propylene and butadiene. The preparation method comprises the following steps of 1, separating n-butane and n-butene from liquefied petroleum gas and 2, respectively carrying out steam cracking on the n-butane and n-butene separated by the step 1 or carrying out steam cracking on a mixture of the n-butane and n-butene. The preparation method has high propylene and butadiene yields.
Description
Technical field
The present invention relates to the preparation method of a kind of propylene and divinyl.
Background technology
Propylene is the important Organic Chemicals being only second to ethene, for the production of multiple important Organic Chemicals, synthetic resins, synthetic rubber and multiple fine chemicals etc., mainly comprise polypropylene, vinyl cyanide, vinylformic acid, isopropyl alkene, acetone, propylene oxide etc., be widely used in national economy every field.At present, the main mode of production of propylene has three kinds: steam cracking process, refinery catalytic cracking technique and dehydrogenating propane technique.Wherein, propylene is mainly derived from steam cracking process, and its output reaches more than 65% of propylene ultimate production, be secondly refinery catalytic cracking technique, and the industrial application of dehydrogenating propane technique is less.In recent years, due to the fast development of propylene derived product, greatly facilitate the quick growth of China to propylene demand.Estimate 2015, the production capacity of China's propylene can reach 2,400 ten thousand tons, and output reaches 2,160 ten thousand tons, and the demand gap dependence on import of about 6,400,000 tons solves.Therefore, China's propylene develops and has broad prospects.
Divinyl is often referred to 1,3-butadiene (also known as ethylene vinyl), for being only second to the important basic petrochemical raw material of ethene and propylene.Divinyl is mainly used in synthetic rubber and resin, as polybutadiene rubber (BR), styrene-butadiene rubber(SBR) (SBR), paracril (NBR), styrene-butadiene polymer latex, styrenic thermoplastic elastomer (SBC) and acrylonitrile-butadiene-styrene (ABS) (ABS) resin etc.In addition, divinyl also can be used for producing the Organic chemical products such as adiponitrile, hexanediamine, nylon-66, BDO, is widely used in numerous areas.
The industrial process of divinyl successively experienced by alcohol dehydrogenase method, butylene catalytic dehydrogenation methods, catalytic dehydrogenation of butanes method, butylene oxidation-dehydrogenation method, ethylene by-product C 4 fraction partition method.At present, the source of divinyl raw material mainly contains two kinds, the hybrid C 4 cut of ethylene cracker by-product and refinery C 4 fraction.In the butadiene production in the whole world, 92% comes from ethylene by-product C 4 fraction partition method, 8% dehydrogenating technology coming from normal butane and n-butene.
At present, on divinyl Downstream Market, the demand of rubber and ABS resin is continuing to increase, divinyl consumption with average annual about 10% speed increment, and production capacity expansion rate of increase less than 8%, the production of divinyl is still in the state that supply falls short of demand.In traditional divinyl preparation technology, the traditional raw material of steam-cracking process is mainly based on lighter hydrocarbons, petroleum naphtha, hydrogenation tail oil, but, the butadiene yield of lighter hydrocarbons steam cracking is less than 3%, the butadiene yield of naphtha steam cracking is 3-6%, and the butadiene yield of hydrogenation tail oil steam cracking is 4-7%.Therefore, with traditional raw material volume increase divinyl approach be very limited.So, constantly expand butadiene production approach, exploitation new raw material and variation route, for ethylene unit and divinyl industry necessary.
Along with the maximization of petroleum chemical enterprise's production equipment scale, the processing power of China's single cover oil refining apparatus is more than 1,000 ten thousand tons/year, and the ethylene production capacity of ethylene unit supporting with it also reaches 80-120 ten thousand tons/year.The output of the liquefied petroleum gas (LPG) (being called for short LPG) that oil refining and ethylene unit are produced improves year by year.At present, the annual production of China's liquefied petroleum gas (LPG) is more than 1,000 ten thousand tons.The liquefied petroleum gas (LPG) of petrochemical enterprise in China by-product is mainly used in the production of civil LPG, only have and produce gasoline and aromatic hydrocarbons for alkylation and aromizing on a small quantity, comprehensive utilization ratio is lower than 15%, well below the U.S., Japan and West Europe more than 50% utilize level, cause the economic value added of liquefied petroleum gas (LPG) resource low.And constantly increase along with the Sweet natural gas consumption of clean domestic fuel, the dim future that liquefied petroleum gas (LPG) uses as fuel.Therefore, make full use of liquefied petroleum gas (LPG) resource, improve its comprehensive utilization ratio and economic value added and become one of important channel of the economic benefit improving Petrochemical Enterprises.
Summary of the invention
The object of the invention is the defect that liquefied petroleum gas (LPG) utilization ratio and Economic Value Added in order to overcome prior art is low, and a kind of method adopting liquefied petroleum gas (LPG) to prepare propylene and divinyl is provided, adopt the method can obtain higher propylene and butadiene yield.
The invention provides the preparation method of a kind of propylene and divinyl, the method comprises the following steps:
(1) from liquefied petroleum gas (LPG), normal butane and n-butene is isolated;
(2) step (1) isolated normal butane and n-butene are carried out steam cracking reaction respectively, or the mixture of described normal butane and n-butene is carried out steam cracking reaction.
As can be seen from the result of embodiment, adopt method of the present invention that the yield of the propylene obtained can be made to reach more than 19.74%, the yield of divinyl reaches more than 7.2%, and the total recovery of propylene and divinyl reaches more than 28.65%.As can be seen here, adopt method provided by the invention can obtain higher propylene and butadiene yield, thus improve utilization ratio and the Economic Value Added of liquefied petroleum gas (LPG).
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Embodiment
Below the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
The preparation method of propylene provided by the invention and divinyl comprises the following steps:
(1) from liquefied petroleum gas (LPG), normal butane and n-butene is isolated;
(2) step (1) isolated normal butane and n-butene are carried out steam cracking reaction respectively, or the mixture of described normal butane and n-butene is carried out steam cracking reaction.
The component of described liquefied petroleum gas (LPG) is known to the skilled person, as a rule, main containing C4 component in described liquefied petroleum gas (LPG), also may contain a small amount of below C3 component and/or more than C5 component.Wherein, below C3 component, in addition may containing a small amount of hydrogen, methane and C2 component mainly containing propane.C4 component, in addition may containing a small amount of iso-butylene and micro-divinyl mainly containing normal butane, Trimethylmethane, n-butene.Wherein, n-butene comprises 1-butylene and 2-butylene, and 2-butylene comprises maleic and anti-butylene.More than C5 component is mainly pentane.According to the difference in source, may there is larger difference in the content of liquefied petroleum gas (LPG) said components.
Be specially adapted in described liquefied petroleum gas (LPG) of the present invention containing Trimethylmethane, normal butane and n-butene; And with the total content of described liquefied petroleum gas (LPG) for benchmark, the content of described Trimethylmethane can be 5-70mol%, the content of described normal butane can be 5-70mol%, and the content of described n-butene can be 10-70mol%; Preferably, with the total content of described liquefied petroleum gas (LPG) for benchmark, the content of described Trimethylmethane is 5-30mol%, and the content of described normal butane is 25-60mol%, and the content of described n-butene is 10-60mol%.In addition, the present invention's liquefied petroleum gas (LPG) used also may contain 1 of below C3 component, more than C5 component, a small amount of iso-butylene and trace, 3-divinyl, with the total content of described liquefied petroleum gas (LPG) for benchmark, the content of described below C3 component can be 5-20mol%, and the content of described more than C5 component can be 0.3-3mol%, and the content of iso-butylene can be 0.1-0.2mol%, the content of described 1,3-butadiene can be 0.01-0.1mol%.
In the present invention, from liquefied petroleum gas (LPG), isolated n-butene comprises 1-butylene and 2-butylene.In actual production process, the mixture of 1-butylene and 2-butylene can be isolated from liquefied petroleum gas (LPG), and the mixture of this 1-butylene and 2-butylene is carried out steam cracking; Also first can isolate 1-butylene and 2-butylene respectively, then 1-butylene and 2-butylene be carried out steam cracking reaction respectively.
The present invention is not particularly limited the method isolating normal butane and n-butene from described liquefied petroleum gas (LPG), such as, can adopt conventional distillation, extracting rectifying, fractionation by adsorption with in chemical separation method any one or to be multiplely separated.
According to a kind of embodiment of the present invention, when containing below C3 component in described liquefied petroleum gas (LPG), Trimethylmethane, normal butane, 1-butylene, iso-butylene, when 2-butylene and more than C5 component, first be separated below C3 component and more than C4 Component seperation by conventional distillation, and more than the C4 component obtained is carried out conventional distillation separation, obtain the mixture of Trimethylmethane and 1-butylene and iso-butylene and the mixture of normal butane and 2-butylene and more than C5 component, again Trimethylmethane is carried out conventional distillation with 1-butylene and the mixture of iso-butylene and be separated the mixture and Trimethylmethane that obtain 1-butylene and iso-butylene, normal butane and 2-butylene and more than C5 component mixture are carried out conventional distillation and is separated the mixture and more than C5 component that obtain normal butane and 2-butylene.Because the boiling point of 1-butylene and iso-butylene is close, the boiling point of normal butane and 2-butylene is close, uses conventional distillation to be separated and is difficult to them to separate, also need to be separated with C 4 fraction fractionation and/or extraction fractional distillation further.
Described C 4 fraction fractionation can be under etherification reaction condition, the mixture of 1-butylene and iso-butylene and methyl alcohol are reacted, make isobutene conversion wherein be methyl tertiary butyl ether (MTBE), and then etherification product is carried out conventional distillation separation, obtain 1-butylene.
Extraction fractional distillation is the principle that utilizes the alkene of C4 and alkane relative volatility in extraction solvent to differ greatly and realizes being separated of alkane and alkene.Extraction smart process in solvent used usually can be in morpholine, N-Methyl pyrrolidone (NMP) and dimethyl formamide (DMF) any one or multiple.At present, extraction fractional distillation can be such as Japanese auspicious father-in-law's extraction fractional distillation or German Krupp-cooper that method (see DE3532289A1).
Particularly, the auspicious father-in-law's extraction fractional distillation of Japan can use DMF and/or NMP as solvent, the extracting system adopted generally includes two extracting rectifying devices and two rectifying tower, and each extracting rectifying device is made up of an extractive distillation column and a solvent recovery tower.The product obtained by first extracting rectifying device removing alkane, and is isolated 2-butylene at the first rectifying tower by C4 component, isolates 1-butylene at Second distillation column.In addition, the second extracting rectifying device is to isolate 1,3-butadiene.Therefore, if not containing 1,3-butadiene in C4 component to be separated, then the second extracting rectifying device can omit.The processing parameter of each extracting rectifying device and rectifying tower is set to as well known to those skilled in the art above, will repeat no more at this.
Germany's your method of Krupp-cooper take n-butene as target product, and raw material is C4 component after etherificate or through etherificate and precise distillation isolates the C4 component after 1-butylene and Trimethylmethane, the solvent adopted is anhydrous morpholine.Particularly, C4 component being introduced fills in the extraction solvent distillation tower of solvent, alkane in C4 component flows out from extraction solvent overhead, and the extraction liquid containing alkene goes out from extraction solvent distillation tower tower bottom flow, and the described extraction liquid containing alkene is obtained olefin component after recycling design in solvent recovery tower.The processing parameter of above extraction solvent distillation tower and solvent recovery tower is set to as well known to those skilled in the art, will repeat no more at this.
It should be noted that, in actual production process, in order to save the cost be separated further, from liquefied petroleum gas (LPG), be separated the normal butane that obtains and n-butene can containing a small amount of impurity, as long as make the content of target separated product be greater than 95 % by weight.Such as, in example 2, in butylene materials at bottom of tower, the flow of 1-butylene is 25.46kg/h, account for 98.87 % by weight of butylene materials at bottom of tower, now, this material directly can be carried out steam cracking as the raw material containing 1-butylene, and without the need to being separated further.
Method provided by the invention also comprises isolates propylene and divinyl from steam cracking reaction product.It should be noted that, when described normal butane and n-butene are carried out steam cracking reaction by the present invention respectively, obtain two kinds of split products, now, first can isolate propylene and divinyl again from the mixture obtained by after two kinds of split product mixing, also these two kinds of split products can be separated respectively.
According to the present invention, described steam cracking reaction and being separated in cracker of split product are carried out.Described cracker comprises pyrolyzer and tripping device.Described pyrolyzer can be the steam cracking propylene of this area routine use and the pyrolyzer of divinyl.Described pyrolyzer mainly comprises convection zone, radiation section, quenching boiler and gas burning system usually.In described pyrolyzer, respectively by cracking stock be steam heated to generation steam cracking reaction, generate the splitting gas containing propylene and divinyl.In the preferred case, described pyrolyzer is preferably tube cracking furnace.Described tube cracking furnace comprises convection zone, radiation section, quenching boiler and gas burning system, and cracking stock enters radiation section in convection zone; In radiation section, cracking stock be steam heated to generation steam cracking reaction, generate the splitting gas containing propylene and divinyl; Splitting gas out enters quenching boiler afterwards from radiation section, and in quenching boiler, splitting gas is cooled to 300-600 DEG C, to make splitting gas scission reaction not occur, reclaims heat simultaneously; Fuel system is used for providing heat to steam cracking reaction process.Described tripping device is used for hydrocarbon splitting gas being separated into different carbon number.As a rule, described tripping device mainly comprises: oil scrubber, water wash column, ice chest, compressor, demethanizing tower, deethanizing column, ethylene rectification tower, depropanizing tower, propylene rectification tower, debutanizing tower, C2 and C3 hydrogenation unit, C2 and C3 rectifying tower, methanation device and butadiene extraction unit.The implementation method of described tripping device has been conventionally known to one of skill in the art, does not repeat them here.
According to the present invention, when described steam cracking reaction carries out in pyrolyzer, in described steam cracking reaction process, the coil outlet temperature of described pyrolyzer is preferably 760-839 DEG C, is more preferably 780-839 DEG C; Water weight of oil, than being preferably 0.3-1, is more preferably 0.35-0.65.In addition, in described steam cracking reaction process, other Parameter Conditions of described pyrolyzer can processing condition conveniently be implemented, and are not particularly limited in the present invention.
Below will be described the present invention by embodiment.
In the following Examples and Comparative Examples, the yield of propylene and divinyl is according to following formulae discovery:
Gross weight × 100% of the weight ÷ steam cracking reaction product of propylene in propene yield (% by weight)=steam cracking reaction product;
Gross weight × 100% of the weight ÷ steam cracking reaction product of divinyl in butadiene yield (% by weight)=steam cracking reaction product;
Total recovery (% by weight)=propene yield+butadiene yield of propylene and divinyl.
In following examples and comparative example, the composition of the liquefied petroleum gas (LPG) LPG used is as shown in table 1:
Table 1
Embodiment 1
This embodiment is for illustration of the preparation method of propylene provided by the invention and iso-butylene.
(1) be separated:
Liquefied petroleum gas (LPG) LPG-1 is introduced described C4 tower with the inlet amount of 100kg/h, the feeding temperature of 40 DEG C, the feed pressure of 11atm in the middle part of C4 tower and carries out rectifying.The parameter of C4 tower is arranged by table 2, and the separating resulting of gained is as shown in table 3.Wherein, the material obtained at the bottom of C4 tower tower is the mixture of normal butane and 2-butylene, and the mass content of normal butane is 86.00%, and the mass content of 2-butylene is 13.96%.The material obtained at the bottom of C4 tower tower is separated by your extraction fractional distillation of German Krupp-cooper, obtains normal butane and 2-butylene respectively.
Table 2
| Numbering | C4 tower |
| Number of theoretical plate | 99.0 |
| Tower top temperature, DEG C | 34.1 |
| Column bottom temperature, DEG C | 57.7 |
| Tower top pressure, atm | 4.5 |
| Tower bottom pressure, atm | 6.0 |
| Reflux ratio | 20.0 |
Table 3
(2) steam cracking reaction:
The normal butane obtain step (1) and 2-butylene are introduced respectively in CBL-III type pyrolyzer (purchased from China PetroChemical Corporation, lower same) and are carried out steam cracking reaction, obtain two kinds of steam cracking products.Then isolate propylene and divinyl after being mixed by two kinds of steam cracking products, and calculate the yield of propylene and divinyl, wherein, the condition of steam cracking reaction is as shown in table 6 below, and result is as shown in table 7.
Embodiment 2
This embodiment is for illustration of the preparation method of propylene provided by the invention and iso-butylene.
(1) be separated:
The separation system adopted comprises C3 tower, C4 tower, C5 tower and butylene tower, liquefied petroleum gas (LPG) LPG-2 is carried out rectifying with the inlet amount of 100kg/h, the feeding temperature of 40 DEG C, the feed pressure of 11atm from the middle part introducing C3 tower of C3 tower, and the product obtained at the bottom of C3 tower tower is carried out rectifying from the middle part introducing C4 tower of C4 tower, product C4 column overhead obtained again is introduced butylene tower from the middle part of butylene tower and is carried out rectifying, the product obtained at the bottom of C4 tower tower is introduced C5 tower in the middle part of C5 tower simultaneously and carry out rectifying, using the material that obtains at the bottom of butylene tower tower as cracking stock 1.Wherein, each tower parameter is arranged by table 4, and the separating resulting of gained is as shown in table 5.The material of C5 column overhead is separated respectively by your extraction fractional distillation of German Krupp-cooper with the material of butylene column overhead, obtains normal butane, 1-butylene and 2-butylene.
Table 4
| Numbering | C3 tower | C4 tower | C5 tower | Butylene tower |
| Number of theoretical plate | 35.0 | 99.0 | 30.0 | 150.0 |
| Tower top temperature, DEG C | 26.8 | 38.2 | 50.8 | 31.99 |
| Column bottom temperature, DEG C | 76.0 | 58.1 | 93.6 | 39.31 |
| Tower top pressure, atm | 10.0 | 4.5 | 5.0 | 4.0 |
| Tower bottom pressure, atm | 10.1 | 6.0 | 5.1 | 4.5 |
| Reflux ratio | 20.0 | 20.0 | 3.0 | 20.0 |
Table 5
(2) steam cracking reaction:
Normal butane, 2-butylene, 1-butylene and the cracking stock 1 step (1) obtained is introduced in CBL-III type pyrolyzer respectively and is carried out steam cracking reaction, then isolate propylene and divinyl after being mixed by several steam cracking products obtained, and calculate the yield of propylene and divinyl.Wherein, the condition of steam cracking reaction is as shown in table 6 below, and result is as shown in table 7.
Embodiment 3
This embodiment is for illustration of the preparation method of propylene provided by the invention and iso-butylene.
Propylene and iso-butylene is prepared according to the method for embodiment 2, unlike, in steam cracking reaction process, the mixture of normal butane, 2-butylene, 1-butylene and cracking stock 1 is introduced in CBL-III type pyrolyzer and carry out steam cracking reaction.Wherein, the condition of steam cracking reaction is as shown in table 6, and result is as shown in table 7.
Comparative example 1
This comparative example is for illustration of the reference preparation method of propylene and divinyl.
Liquefied petroleum gas (LPG) LPG-1 is directly sent in CBL-R type pyrolyzer and carry out steam cracking reaction, obtain steam cracking product, then from steam cracking product, isolate propylene and divinyl, and calculate the yield of propylene and divinyl.Wherein, the condition of steam cracking reaction is as shown in table 6 below, and result is as shown in table 7.
Comparative example 2
This comparative example is for illustration of the reference preparation method of propylene and divinyl.
Liquefied petroleum gas (LPG) LPG-2 is directly sent in CBL-R type pyrolyzer and carry out steam cracking reaction, obtain steam cracking product, then from steam cracking product, isolate propylene and divinyl, and calculate the yield of propylene and divinyl.Wherein, the condition of steam cracking reaction is as shown in table 6 below, and result is as shown in table 7.
Table 6
Table 7
As can be seen from the data of table 7, adopt method of the present invention can significantly improve the yield of propylene and divinyl.Particularly, the steam crack material used in embodiment 1-3 is for being separated the normal butane and n-butene that obtain, and the steam crack material used in comparative example 1-2 is respectively LPG-1 and LPG-2, acetonideexample 1-3 obtains obviously higher propylene and butadiene yield, thus solves existing liquefied petroleum gas (LPG) utilization ratio and the low problem of Economic Value Added.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (7)
1. a preparation method for propylene and divinyl, the method comprises the following steps:
(1) from liquefied petroleum gas (LPG), normal butane and n-butene is isolated;
(2) step (1) isolated normal butane and n-butene are carried out steam cracking reaction respectively, or the mixture of described normal butane and n-butene is carried out steam cracking reaction.
2. method according to claim 1, wherein, containing Trimethylmethane, normal butane and n-butene in described liquefied petroleum gas (LPG); And with the total content of described liquefied petroleum gas (LPG) for benchmark, the content of described Trimethylmethane is 5-70mol%, the content of described normal butane is 5-70mol%, and the content of described n-butene is 10-70mol%.
3. method according to claim 2, wherein, with the total content of described liquefied petroleum gas (LPG) for benchmark, the content of described Trimethylmethane is 5-30mol%, and the content of described normal butane is 25-60mol%, and the content of described n-butene is 10-60mol%.
4. according to the method in claim 1-3 described in any one, wherein, described steam cracking reaction carries out in pyrolyzer, and in described steam cracking reaction process, the coil outlet temperature of described pyrolyzer is 760-839 DEG C, and water weight of oil is than being 0.3-1.
5. method according to claim 4, wherein, in described steam cracking reaction process, the coil outlet temperature of described pyrolyzer is 780-839 DEG C, and water weight of oil is than being 0.35-0.65.
6. method according to claim 4, wherein, described pyrolyzer is tube cracking furnace.
7. according to the method in claim 1-3 described in any one, wherein, the method also comprises isolate propylene and divinyl from described steam cracking product.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2873301A (en) * | 1956-04-09 | 1959-02-10 | Sinclair Refining Co | Thermal process for preparing butadiene from butene-2 |
| US20040186335A1 (en) * | 2002-04-23 | 2004-09-23 | Jong-Hyun Chae | Process for pyrolysis of hydrocarbon |
| CN1668556A (en) * | 2002-07-12 | 2005-09-14 | 巴斯福股份公司 | Method for the production of butadiene from n-butane |
| CN101734990A (en) * | 2008-11-25 | 2010-06-16 | 中国石油天然气股份有限公司 | Method for preparing ethylene by steam cracking of tubular cracking furnace |
-
2013
- 2013-06-28 CN CN201310270179.8A patent/CN104250193B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2873301A (en) * | 1956-04-09 | 1959-02-10 | Sinclair Refining Co | Thermal process for preparing butadiene from butene-2 |
| US20040186335A1 (en) * | 2002-04-23 | 2004-09-23 | Jong-Hyun Chae | Process for pyrolysis of hydrocarbon |
| CN1668556A (en) * | 2002-07-12 | 2005-09-14 | 巴斯福股份公司 | Method for the production of butadiene from n-butane |
| CN101734990A (en) * | 2008-11-25 | 2010-06-16 | 中国石油天然气股份有限公司 | Method for preparing ethylene by steam cracking of tubular cracking furnace |
Non-Patent Citations (2)
| Title |
|---|
| 周禹: "由液化石油气生产烯烃及其衍生物", 《燕山石化》, no. 4, 31 December 1984 (1984-12-31), pages 286 - 300 * |
| 王翰舟、钱伯章: "增产丙烯的技术进展", 《石油化工》, vol. 29, no. 9, 31 December 2000 (2000-12-31), pages 705 - 711 * |
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