CN101130472A - Method and apparatus for steam dealkylation of hydrocarbons in an olefin plant - Google Patents

Method and apparatus for steam dealkylation of hydrocarbons in an olefin plant Download PDF

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Publication number
CN101130472A
CN101130472A CNA2007101426196A CN200710142619A CN101130472A CN 101130472 A CN101130472 A CN 101130472A CN A2007101426196 A CNA2007101426196 A CN A2007101426196A CN 200710142619 A CN200710142619 A CN 200710142619A CN 101130472 A CN101130472 A CN 101130472A
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fraction
steam dealkylation
dealkylation
described method
hydrogen
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H·弗里茨
V·格克
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Linde GmbH
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Linde GmbH
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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Abstract

The present invention describes a method for treating fractions (C7+ fractions) composed of hydrocarbon containing seven carbon atoms, the fraction is formed in a device for generating hydrocarbon by means of steam cracking of hydrocarbon-containing feeding (alkene device), as well as an apparatus for applying the method. After hydrogenation, feeding the C7+ fractions for steam dealkylation, so as to generate usable product benzene and hydrogen.

Description

The method and apparatus that is used for steam dealkylation hydro carbons in olefin hydrocarbon apparatus
Technical field
The present invention relates to be used to handle main fraction (C by hydrocarbon composition with at least 7 carbon atoms 7+Fraction) method, this fraction are (olefin hydrocarbon apparatus) that is formed by the steam cracking of hydrocarbonaceous feed in being used to produce the device of hydro carbons, and the equipment that is used to implement this method.
Background technology
In the olefin hydrocarbon apparatus that is used for the steam cracking hydrocarbonaceous feed, with hydrocarbonaceous feed and vapor mixing, and be heated to very high temperature (about 850 ℃) in short-term, thereby make the generate longer-chain hydrocarbons in the feed material be cracked into short-chain hydrocarbons.These short-chain hydrocarbons (mainly being ethene) are the primary products of this type of device.But also produce a series of by product extraly, their relative proportion and composition depend on the composition of hydrocarbonaceous feed.
A kind of main by product is so-called pyrolysis gasoline (Pyrolsebenzin).It has intensive aromaticity (30% benzene, 15% toluene, 20% C8 aromatic hydrocarbons), contains many alkene and conjugated diene, and be in device from remaining product stream as main fraction (C by hydrocarbon composition with at least 5 carbon atoms 5+Fraction) isolated.As the component that can use economically, C 5+Fraction contains aromatic hydrocarbons, and it is used as the initial substance of synthetic many plastics, and is used to improve the antiknock value of gasoline.According to prior art, to C 5+Fraction is implemented first selective hydration, wherein makes diolefine become its corresponding alkene or ethylbenzene with styrene conversion.Subsequently with C 5+The fraction fractionation by distillation becomes a kind of fraction and a kind of fraction (C that mainly contains the hydro carbons with at least 6 carbon atoms that mainly contains the hydro carbons with 5 carbon atoms 6+Fraction).To the C that produces 6+Fraction is implemented hydrogenation contains sulphur, nitrogen and/or oxygen with conversion and separation component.According to prior art, with present hydrogenant C 6+The fraction fractionation by distillation becomes a kind of fraction and a kind of fraction (C that mainly contains the hydro carbons with at least 7 carbon atoms that mainly contains the hydro carbons with 6 carbon atoms 7+Fraction).Utilize extracting rectifying to obtain the benzene that can use economically by this fraction that mainly contains hydro carbons with 6 carbon.In order to improve the productive rate of benzene, according to prior art also to C 7+Fraction is implemented the hydrogen dealkylation.
For example WO 2005/071045 has described this type of and has been used for the method for hydrogen dealkylation.Exist under the situation of catalyzer in 400 to 650 ℃ temperature and 20 crust to the pressure of 40 crust, to make C 7+Fraction contacts with hydrogen, and wherein hydrogen exists with 3 to 6 times of molar excess of hydro carbons.Under these conditions, take off alkyl, thereby form benzene and various alkane (for example methane and ethane) from each alkylating aromatic hydrocarbons (for example toluene and dimethylbenzene) branch.
At C 7+The consumption of hydrogen and the extracting rectifying of complexity that mainly contains the fraction of the hydro carbons with 6 carbon atoms during the hydrogen dealkylation of fraction have negative impact according to prior art with the economy of the method that obtains benzene for these.
Therefore, the objective of the invention is to develop selection at a kind of economy of prior art.
Summary of the invention
This purpose is to pass through C according to the present invention aspect method 7+Fraction is implemented steam dealkylation and is realized, wherein except such as two kinds of spendable product material benzene of main generation and the hydrogen reaction product of carbon monoxide and carbonic acid gas.
Basic thought of the present invention is by means of steam dealkylation alkylating aromatic hydrocarbons to be implemented dealkylation to produce benzene.Steam dealkylation only needs water vapor with low cost as feed material, and also produces valuable by product hydrogen except desired valuable product benzene.
Embodiment
The C that is used for steam dealkylation 7+Fraction mainly contains
A) have the aromatic hydrocarbons of 7 to 10 carbon atoms,
B) have the cyclic paraffins (naphthenic hydrocarbon) of 6 to 10 carbon atoms,
C) have the different paraffin and the positive paraffin of 6 to 10 carbon atoms,
D) have the alkene of 7 to 10 carbon atoms, or
Any mixture of aforementioned substances, wherein the accurate composition of mixture depends on the various hydrocarbonaceous feed of olefin hydrocarbon apparatus.The ratio of aromatic hydrocarbons obviously is less than the aforementioned charging that contains generate longer-chain hydrocarbons in the cracked gas of being made up of aforementioned short-chain hydrocarbons in the steam cracking of olefin hydrocarbon apparatus that charging had.But the method according to this invention is suitable for C 7+The various described composition of fraction.
From C 7+The hydro carbons of fraction preferably reacts on solid catalyst under the situation of input heat in gas phase with water vapor.Exist vaporous water (steam) under the situation that is continuing the input heat on the catalyzer, to make gaseous state C 7+The fraction dealkylation, thus desired product benzene and hydrogen except carbon monoxide, carbonic acid gas and other by products, formed.
The required heat of dealkylation reaction preferably produces by the burning of feed material and air.From vapor reaction by product, especially carbon monoxide and the methane of steam dealkylation, being used for burning with air as charging also is proved to be particularly preferred.From a part of vapor reaction by product, especially carbon monoxide and the methane of steam dealkylation, be combustible, thereby can produce required heat of reaction to burn as feed material.Therefore, store heat gas, and these other untapped part of reaction product sent into suitable purposes.
Purpose ground is separated into gaseous hydrogen and vapor reaction by product, especially carbon monoxide, carbonic acid gas and methane through pressure-exchange absorption with gaseous reaction products after compression.Valuable by product hydrogen exists with gaseous state equally, and can have a mind to very much the free burial ground for the destitute be used for the burning.By comprising the pressure-exchange absorption of aforementioned compression, make hydrogen easily with the combustible vapor reaction separation of by-products that can be used as aflame charging.
The flue gas that forms in burning preferably is cooled under the situation of the feed material of heating steam dealkylation through heat exchanger.Feed material (the C of the pre-heated from heat steam dealkylation by utilizing flue gas 7+Fraction and steam), also reduced in order to keep the required temperature heat necessary to be imported of dealkylation reaction.Thereby realized the economic utilization of the energy.
C 7+Fraction and water vapor preferably in pipeline, more preferably from top to bottom, process on solid catalyst, wherein catalyzer is positioned at pipe interior.Purpose ground is with the outside heat input channel.The required heat of dealkylation reaction preferably is transported on the pipeline by electromagnetic radiation, thermal radiation and/or convection current.Real dealkylation is reflected at the pipe interior that wherein has catalyzer to carry out.Guide two kinds of reaction partner (C 7+Fraction and steam) from top to bottom by pipeline with the catalyzer filling.The required heat of dealkylation reaction produces in the pipeline outside, and the described mechanical transport of process utilizes thermal conduction and convection current that heat delivery is entered on the response location of pipe interior to pipeline thus.
The preferred solid catalyst that uses is made up of following material: porous carrier materials, especially γ-Al 2O 3, magnesium-aluminium spinel and/or Cr 2O 3, and be positioned at activeconstituents on the surfaces of carrier materials, especially have the Rh of 0.1 to 1.0 weight % adsorption concentration (Beladung) and/or have the Pd of 0.2 to 2.0 weight % adsorption concentration.
Preferably at 400 ℃ to 600 ℃, more preferably 450 ℃ to 550 ℃, preferred especially 480 ℃ to 520 ℃ temperature and 1 to 15 crust more preferably 1.2 to 10 cling to, and the pressure of preferred especially 1.5 to 8 crust are implemented steam dealkylation down.
The mol ratio of purpose ground water vapor and hydro carbons in entering reactor the time is implemented steam dealkylation 1 to 20 under the situation in preferred 2 to 15 the scope.In another embodiment of the invention, the mol ratio of water vapor and hydro carbons is implemented steam dealkylation 3 to 12 under the situation in preferred 5 to 10 the scope in the time of in entering reactor.Generally speaking, implement steam dealkylation under the situation of water molar excess, wherein the accurate ratio in different embodiments of the present invention depends on C 7+The accurate composition of fraction.
Before steam dealkylation to C 7+Fraction implements to be used to transform diolefine and cinnamic method is proved to be favourable, wherein especially adopts the method for hydrogenation that consumes hydrogen for this reason.In another embodiment of the invention, before steam dealkylation with C 7+Fraction is separated from the fraction of hydro carbons with at least 6 carbon atoms, wherein the fraction of hydro carbons with at least 6 carbon atoms is implemented to be used to transform diolefine and cinnamic method, especially consumes the method for hydrogenation of hydrogen.Before steam dealkylation to C 7+Fraction is implemented to be used to transform and the method for separating the component that contains sulphur, nitrogen and/or oxygen also is favourable, wherein especially adopts the method for hydrogenation that consumes hydrogen for this reason.By adopting method for hydrogenation, can be with C 7+The diolefine that exists in the fraction is converted into its corresponding alkene, equally also can transform and separates the component that contains sulphur, nitrogen and/or oxygen.Thus, avoided catalyzer deactivate and significant prolongation the working time of catalyzer (Laufzeit).At this, depend on embodiment of the present invention, C 7+Fraction itself can be hydrogenated or from hydrogenant C 6+Fraction is separated.
The reaction product of preferred cooling steam dealkylation, and in 3 are separated, be separated into gaseous reaction products, hydro carbons and water.Reaction product from steam dealkylation not only contains desired valuable product benzene and hydrogen, but also contains reaction product and byproduct of reaction such as carbon monoxide and carbonic acid gas.In order to obtain desired valuable product, must reaction product isolated.Be separated through 3 the refrigerative reaction product is separated into the especially hydro carbons and the water of gaseous reaction products, the especially benzene of hydrogen, carbon monoxide, carbonic acid gas and methane.
Purpose ground will be at C 7+The hydrogen that forms in the steam dealkylation of fraction is completely or partially delivered in the charging of the method that consumes hydrogen.The hydrogen that produces completely or partially can be used for the method for foregoing consumption hydrogen in steam dealkylation, thereby the demand to outside hydrogen to be imported is minimized.
In another embodiment of the invention, will be at C 7+The hydrogen that forms in the steam dealkylation of fraction is delivered to arbitrarily the product of other olefin hydrocarbon apparatus that consume hydrogen and the hydrogenation process of by product as charging, and is saturated in particular for making mainly by the fraction of the hydrocarbon composition with 4 or more a plurality of carbon atoms.C 7+The hydrogenation of fraction is not the method for the consumption hydrogen of some olefin hydrocarbon apparatus.The method for hydrogenation that needs the primary product of olefin hydrocarbon apparatus equally can use the hydrogen that produces for this reason equally in steam dealkylation.
In another embodiment of the invention, will be at C 7+The hydrogen that forms in the steam dealkylation of fraction is delivered to refinery as charging.
For good productive rate from the desired reaction product benzene of steam dealkylation, before steam dealkylation with C 7+Sulphur content in the fraction is reduced to and is lower than 10ppm, preferably is lower than 3ppm, especially preferably is lower than 1ppm, is proved to be favourable.
Preferably isolate benzene from the hydro carbons of reaction product through rectifying.Preferably benzene is implemented the meticulous purification of adsorptivity with dry and removal trace components after the rectifying, wherein carry benzene through sorbent material, trace components and benzene are adsorbed on the contrary on sorbent material.By adopting the method according to this invention, can obtain benzene from reaction product by simple rectifying, and further process or put on market.Do not need complicated extraction or extracting rectifying, for example adopt method, thereby reduced cost of investment and method cost according to prior art.
C 7+Preferably being transformed in the fraction by steam dealkylation with benzene boiling point component approaching or that form azeotropic mixture.Purpose ground will be chosen wantonly from all reaction product of mainly being made up of the unconverted feed material of steam dealkylation than the more difficult ebullient of benzene of rectifying and send back in the steam dealkylation process as feed material through over hydrogenation.In another embodiment of the invention, will mainly before steam dealkylation, send C back to than the more difficult ebullient of benzene from all of rectifying by the reaction product that the unconverted feed material of steam dealkylation is formed 7+Fraction, C 6+The hydrogenation process of fraction or mainly by the hydrogenation process of the fraction of hydrocarbon composition with at least 5 carbon atoms.By unconverted feed material being sent back to hydrogenation process or steam dealkylation process, realized circulation, and can not lose valuable feed material.
In another embodiment of the invention, before steam dealkylation, will have the fraction and the C of the hydro carbons of at least 8 carbon atoms 7+The fraction fractionation by distillation is wherein implemented steam dealkylation separately to isolated fraction with hydro carbons of at least 8 carbon atoms.In this embodiment of the present invention, p-Xylol (mainly being contained in the fraction of isolated hydro carbons with at least 8 carbon atoms) and toluene (mainly are contained in residual C 7+In the fraction) implement steam dealkylation separately.
The purpose that is proposed is to realize by the equipment of the stove that comprises the pipeline that has the combustion chamber and be positioned at the combustion chamber aspect equipment.Real steam dealkylation is to implement at the pipeline of the combustion chamber that is arranged in this stove, can produce the required heat of dealkylation reaction at this.
Be installed in the combustion chamber to the pipeline preferred vertical, and in the lower end and/or the upper end have the temperature compensation element.The lower end of vertical ducting and/or the temperature compensation element on the upper end have stoped the mechanical stress of the loss raising that can cause pipeline by the temperature difference.
Purpose ground, each pipeline has C 7+The input unit of fraction and water vapor and the take-off equipment of reaction product.
Each pipe interior is filled with catalyzer and also is proved to be favourable, and wherein catalyzer is made up of following material: porous carrier materials, especially γ-Al 2O 3, magnesium-aluminium spinel and/or Cr 2O 3, and be positioned at activeconstituents on the surfaces of carrier materials, especially have the Rh of 0.1 to 1.0 weight % adsorption concentration (Beladung) and/or have the Pd of 0.2 to 2.0 weight % adsorption concentration.
Stove preferably on wall, covering and/or having at least one burner in the bottom.This pipeline of purpose ground is suitable for 1 to 15 crust, preferred 1.2 to 10 crust, and the interior pressure of preferred especially 1.5 to 8 crust, and be applicable in the stove with the highest 1400 ℃ flame temperature.
Especially can be provided for handling C by the present invention 7+The selection at other economy of prior art of fraction.By adopting the method according to this invention and, except spendable product benzene, also producing valuable by product hydrogen according to equipment of the present invention.

Claims (35)

1. be used to handle main fraction (C by hydrocarbon composition with at least 7 carbon atoms 7+Fraction) method, this fraction are (olefin hydrocarbon apparatus) that is produced by the steam cracking of hydrocarbonaceous feed in being used to produce the device of hydro carbons, it is characterized in that, to this C 7+Fraction is implemented steam dealkylation, except such as two kinds of spendable product material benzene of main generation and the hydrogen reaction product of carbon monoxide and carbonic acid gas.
2. method according to claim 1 is characterized in that, described C 7+Fraction mainly contains:
A) have the aromatic hydrocarbons of 7 to 10 carbon atoms,
B) have the cyclic paraffins (naphthenic hydrocarbon) of 6 to 10 carbon atoms,
C) have the different paraffin and the positive paraffin of 6 to 10 carbon atoms,
D) have the alkene of 7 to 10 carbon atoms, or
Any mixture of aforementioned substances.
3. method according to claim 1 and 2 is characterized in that, from described C 7+The hydro carbons of fraction and water vapor react on solid catalyst under the situation of input heat in gas phase.
4. according to the described method of one of claim 1 to 3, it is characterized in that the required heat of described dealkylation reaction burns by feed material and air and produces.
5. according to the described method of one of claim 1 to 4, it is characterized in that, the gaseous reaction products of described steam dealkylation is separated into gaseous hydrogen and vapor reaction by product, especially carbon monoxide, carbonic acid gas and methane through pressure-exchange absorption after compression.
6. according to the described method of one of claim 1 to 5, it is characterized in that, will be used for and air combustion as feed material from vapor reaction by product, especially carbon monoxide and the methane of described steam dealkylation.
7. according to the described method of one of claim 1 to 6, it is characterized in that the flue gas that produces is cooled under the situation of the feed material of the described steam dealkylation of heating through heat exchanger when burning.
8. according to the described method of one of claim 1 to 7, it is characterized in that described C 7+Fraction and water vapor in pipeline, preferably from top to bottom, process on solid catalyst, wherein this catalyzer is positioned at this pipe interior.
9. according to the described method of one of claim 1 to 8, it is characterized in that, the heat of outside is imported described pipeline.
10. method according to claim 9 is characterized in that, the required heat of described dealkylation reaction is transported on the described pipeline by electromagnetic radiation, thermal radiation and/or convection current.
11., it is characterized in that used solid catalyst is made up of following material according to the described method of one of claim 1 to 10: porous carrier materials, especially γ-Al 2O 3, magnesium-aluminium spinel and/or Cr 2O 3, and be positioned at activeconstituents on this surfaces of carrier materials, especially have the Rh of 0.1 to 1.0 weight % adsorption concentration and/or have the Pd of 0.2 to 2.0 weight % adsorption concentration.
12. according to the described method of one of claim 1 to 11, it is characterized in that,, more preferably 450 ℃ to 550 ℃, implement described steam dealkylation under preferred especially 480 ℃ to the 520 ℃ temperature at 400 ℃ to 600 ℃.
13., it is characterized in that at 1 to 15 crust, more preferably 1.2 to 10 crust are implemented described steam dealkylation under the pressure of preferred especially 1.5 to 8 crust according to the described method of one of claim 1 to 12.
14., it is characterized in that the mol ratio of water vapor and hydro carbons is implemented described steam dealkylation 1 to 20 in the time of in entering reactor under the situation in preferred 2 to 15 the scope according to the described method of one of claim 1 to 13.
15., it is characterized in that the mol ratio of water vapor and hydro carbons is implemented described steam dealkylation 3 to 12 in the time of in entering reactor under the situation in preferred 5 to 10 the scope according to the described method of one of claim 1 to 14.
16. according to the described method of one of claim 1 to 15, it is characterized in that, before described steam dealkylation to described C 7+Fraction implements to be used to transform diolefine and cinnamic method, especially adopts the method for hydrogenation that consumes hydrogen for this reason.
17. according to the described method of one of claim 1 to 16, it is characterized in that, before described steam dealkylation with described C 7+Fraction is from the fraction (C of hydro carbons with at least 6 carbon atoms 6+Fraction) separates, this C 6+Fraction is implemented to be used to transform diolefine and cinnamic method, especially consumes the method for hydrogenation of hydrogen.
18. according to the described method of one of claim 1 to 17, it is characterized in that, before described steam dealkylation to described C 7+The method that fraction enforcement is used to transform and separate the component that contains sulphur, nitrogen and/or oxygen especially adopts the method for hydrogenation that consumes hydrogen for this reason.
19., it is characterized in that according to the described method of one of claim 1 to 18, cool off the reaction product of described steam dealkylation, and in 3 are separated, be separated into gaseous reaction products, hydro carbons and water.
20. according to the described method of one of claim 1 to 19, it is characterized in that, will be at described C 7+The hydrogen that forms in the steam dealkylation of fraction is completely or partially delivered in the charging according to the method for claim 16 or 17 described consumption hydrogen.
21. according to the described method of one of claim 1 to 20, it is characterized in that, will be at described C 7+The hydrogen that forms in the steam dealkylation of fraction is delivered to arbitrarily the product of other olefin hydrocarbon apparatus that consume hydrogen and the hydrogenation process of by product as charging, and is saturated in particular for making mainly by the fraction of the hydrocarbon composition with 4 or more a plurality of carbon atoms.
22. according to the described method of one of claim 1 to 21, it is characterized in that, will be at described C 7+The hydrogen that forms in the steam dealkylation of fraction is delivered to refinery as charging.
23. according to the described method of one of claim 1 to 22, it is characterized in that, before described steam dealkylation with described C 7+Sulphur content in the fraction is reduced to and is lower than 10ppm, preferably is lower than 3ppm, especially preferably is lower than 1ppm.
24. according to the described method of one of claim 1 to 23, it is characterized in that, isolate benzene from the hydro carbons of reaction product through rectifying.
25. method according to claim 24 is characterized in that, after the rectifying benzene is implemented the meticulous purification of adsorptivity with dry and removal trace components, carries benzene through sorbent material, this trace components of absorption on this sorbent material.
26. according to the described method of one of claim 1 to 25, it is characterized in that, with described C 7+Transform by described steam dealkylation with benzene boiling point component approaching or that form azeotropic mixture in the fraction.
27. according to the described method of one of claim 24 to 26, it is characterized in that, will choose wantonly from all reaction product of mainly forming than the more difficult ebullient of benzene of rectifying and send back in the described steam dealkylation process as feed material through over hydrogenation by the unconverted feed material of described steam dealkylation.
28. according to the described method of one of claim 24 to 26, it is characterized in that, will mainly before described steam dealkylation, send C back to than the more difficult ebullient of benzene from all of rectifying by the reaction product that the unconverted feed material of described steam dealkylation is formed 7+Fraction, C 6+The hydrogenation process of fraction or mainly by the hydrogenation process of the fraction of hydrocarbon composition with at least 5 carbon atoms.
29., it is characterized in that before described steam dealkylation, having the fraction and the described C of the hydro carbons of at least 8 carbon atoms according to the described method of one of claim 1 to 28 7+The fraction fractionation by distillation is implemented described steam dealkylation separately to isolated fraction with hydro carbons of at least 8 carbon atoms.
30. be used to handle main fraction (C by hydrocarbon composition with at least 7 carbon atoms 7+Fraction) equipment, this fraction are (olefin hydrocarbon apparatus) that is produced by the steam cracking of hydrocarbonaceous feed in being used to produce the device of hydro carbons, it is characterized in that this equipment comprises the stove of the pipeline that has the combustion chamber and be positioned at this combustion chamber.
31. equipment according to claim 30 is characterized in that, described pipeline vertically is installed in the described combustion chamber, and in the lower end and/or the upper end have the temperature compensation element.
32., it is characterized in that each described pipeline has and is used for described C according to claim 30 or 31 described equipment 7+The input unit of fraction and water vapor and the take-off equipment of reaction product.
33., it is characterized in that each described pipe interior is filled with catalyzer according to the described equipment of one of claim 30 to 32, this catalyzer is made up of following material: porous carrier materials, especially γ-Al 2O 3, magnesium-aluminium spinel and/or Cr 2O 3, and be positioned at activeconstituents on this surfaces of carrier materials, especially have the Rh of 0.1 to 1.0 weight % adsorption concentration and/or have the Pd of 0.2 to 2.0 weight % adsorption concentration.
34. according to the described equipment of one of claim 30 to 33, it is characterized in that, described stove on wall, covering and/or having at least one burner in the bottom.
35., it is characterized in that described pipeline is suitable for 1 to 15 crust according to the described equipment of one of claim 30 to 34, preferred 1.2 to 10 crust, the interior pressure of preferred especially 1.5 to 8 crust, and be applicable in the stove with the highest 1400 ℃ flame temperature.
CNA2007101426196A 2006-08-18 2007-08-20 Method and apparatus for steam dealkylation of hydrocarbons in an olefin plant Pending CN101130472A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102006038893 2006-08-18
DE102006038893.3 2006-08-18
DE102006058528.3 2006-12-12

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CN101130472A true CN101130472A (en) 2008-02-27

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Application publication date: 20080227